CN203750518U - Fluidic aeration three-phase homogeneous reactor - Google Patents
Fluidic aeration three-phase homogeneous reactor Download PDFInfo
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- CN203750518U CN203750518U CN201420093569.2U CN201420093569U CN203750518U CN 203750518 U CN203750518 U CN 203750518U CN 201420093569 U CN201420093569 U CN 201420093569U CN 203750518 U CN203750518 U CN 203750518U
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- 238000005273 aeration Methods 0.000 title claims abstract description 85
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000002002 slurry Substances 0.000 claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 34
- 238000002347 injection Methods 0.000 claims description 58
- 239000007924 injection Substances 0.000 claims description 58
- 239000001257 hydrogen Substances 0.000 claims description 54
- 229910052739 hydrogen Inorganic materials 0.000 claims description 54
- 238000009826 distribution Methods 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 abstract description 41
- 238000006243 chemical reaction Methods 0.000 abstract description 32
- 239000007788 liquid Substances 0.000 abstract description 17
- 239000000203 mixture Substances 0.000 abstract description 11
- 239000007787 solid Substances 0.000 abstract description 4
- 238000009792 diffusion process Methods 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 90
- 239000003921 oil Substances 0.000 description 60
- 238000005984 hydrogenation reaction Methods 0.000 description 34
- 238000005087 graphitization Methods 0.000 description 21
- 238000000034 method Methods 0.000 description 17
- 239000000047 product Substances 0.000 description 16
- 239000003575 carbonaceous material Substances 0.000 description 13
- 238000002156 mixing Methods 0.000 description 12
- 239000011148 porous material Substances 0.000 description 12
- 239000002184 metal Substances 0.000 description 10
- 229910052751 metal Inorganic materials 0.000 description 10
- 150000002431 hydrogen Chemical class 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 6
- 239000000295 fuel oil Substances 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000003610 charcoal Substances 0.000 description 4
- 238000002513 implantation Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- WURBVZBTWMNKQT-UHFFFAOYSA-N 1-(4-chlorophenoxy)-3,3-dimethyl-1-(1,2,4-triazol-1-yl)butan-2-one Chemical compound C1=NC=NN1C(C(=O)C(C)(C)C)OC1=CC=C(Cl)C=C1 WURBVZBTWMNKQT-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000000498 ball milling Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 150000001723 carbon free-radicals Chemical class 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 229910000428 cobalt oxide Inorganic materials 0.000 description 2
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical group [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000021615 conjugation Effects 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000007598 dipping method Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- -1 naphtha Substances 0.000 description 2
- 238000005554 pickling Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 238000010237 hybrid technique Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- OUUQCZGPVNCOIJ-UHFFFAOYSA-N hydroperoxyl Chemical compound O[O] OUUQCZGPVNCOIJ-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000116 mitigating effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- 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 relates to a fluidic aeration three-phase homogeneous reactor. A fluidic aeration three-phase homogenizing plate is arranged at the bottom of a reactor shell or in a slurry inlet channel, and micropores running through the fluidic aeration three-phase homogenizing plate are formed in the fluidic aeration three-phase homogenizing plate, so that gas bubbles and liquid drops are fine and uniform after a three-phase mixture of oil products, hydrogen gas and catalysts flow through the micropores and can facilitate mutual diffusion and full contact of gas, liquid and solid substances. The fluidic aeration three-phase homogeneous reactor can fully and uniformly mix the oil products, the hydrogen gas and the catalysts, so that the oil products and the hydrogen gas can be in full contact for reacting on the surfaces of the catalysts, the full reaction is achieved and the reaction efficiency is high.
Description
Technical field
The utility model relates to a kind of jet-flow aeration three-phase homogeneous reactor, belongs to hydrogenation catalyst technical field.
Background technology
In petroleum industry production, the chemical reaction of many high-temperature hydrogenations need to be synthesized and be obtained by heterogeneous catalytic reaction.Existing catalytic multi-phase reactor is divided and can be divided into two large classes according to the state of solid catalyst: the reactor of inactive state and the reactor of flow regime.Wherein, the reactor that catalyst remains static has fixed bed reactors, and catalyst has fluidized-bed reactor, moving-burden bed reactor and paste state bed reactor etc. in the reactor of flow regime.
At present for the paste state bed reactor that is mostly in heavy oil high-pressure hydrogenation field, and the paste state bed reactor that can be used in high-pressure hydrogenation field mainly comprises two types of circulation flow reactor and three phase slurry bed bioreactors.Wherein, the course of reaction of circulation flow reactor is difficult to control, and easily produces the phenomenon of a large amount of liquid dispersions, cause the conversion ratio inequality of all kinds of oil products, and the internals of circulation flow reactor is more, and device structure is comparatively complicated.And although three phase slurry bed bioreactor has, temperature is evenly easily controlled, gas speed opereating specification is wide, advantages of simple structure and simple.But it is higher with the uniformity requirement that hydrogen, catalyst mix to raw material, after catalyst, oil product and hydrogen fully need to being mixed, guarantee hydrogen and oil product fully react at catalyst surface, and need hydrogen to be dissolved to rapidly in oil product, the effect of competence exertion hydrogen hydrogenation, to having relatively high expectations of hybrid technique.
In prior art, China document CN103285784A discloses the synthetic three phase slurry bed of a kind of Fischer-Tropsch and reactor thereof, the synthetic three phase slurry bed of this Fischer-Tropsch and reactor thereof comprise reactor shell and are arranged on the air inlet distributor of this reactor shell bottom, on the sidewall of reactor shell, be provided with make-up gas distributor, make-up gas distributor comprises the air inlet pipe outside the sidewall that passes reactor shell, this air inlet pipe comprises main road pipeline and bypass line, described main road pipeline has the air inlet section that is positioned at described reactor enclosure external body and the dispensing section that is positioned at described reactor shell inside, described bypass line is arranged on described dispensing section and with described dispensing section and communicates.Above-mentioned three phase slurry bed bioreactor is by arranging the structure that this make-up gas distributor is perforate on pipe, and object is to improve dispersiveness and the controllability of gas phase, and then promotes the uniformity coefficient that gas, liquid, solid three-phase mixes.But the structure setting of above-mentioned make-up gas distributor can not ensure the uniformity of distributed gas in same level, and because the change of gas flow rate can affect the uniformity that bubble that distributor blows out distributes diametrically, and just for simple gas phase being delivered to the mixing of liquid Space, therefore above-mentioned three-phase slurry reactor can not realize the full and uniform mixing of gas, liquid, solid three-phase, and then directly affected the efficiency of reacting, cause the efficiency of reaction lower.
Utility model content
Technical problem to be solved in the utility model is that three phase slurry bed bioreactor of the prior art is difficult to realize the full and uniform mixing of gas, liquid, solid three-phase, reaction efficiency is low, thereby proposes a kind of even mixing and the high jet-flow aeration three-phase homogeneous reactor of reaction efficiency that can realize oil product, hydrogen and catalyst three-phase.
For solving the problems of the technologies described above, the technical solution of the utility model is as follows:
A kind of jet-flow aeration three-phase homogeneous reactor, comprising:
Reactor shell, is connected with slurry intake channel with the bottom of described reactor shell, is connected with discharging channel with the top of described reactor shell;
In described reactor shell and be positioned at the bottom of described reactor shell, or in described slurry intake channel, be provided with jet-flow aeration three-phase homogeneous plate, on described jet-flow aeration three-phase homogeneous plate, be furnished with micropore, described micropore runs through the setting of described jet-flow aeration three-phase homogeneous plate.
Described jet-flow aeration three-phase homogeneous plate is arranged in described slurry intake channel, the transverse cross-section parallel setting of described jet-flow aeration three-phase homogeneous plate and described slurry intake channel.
Described jet-flow aeration three-phase homogeneous plate is arranged in described reactor shell and is positioned at the bottom of described reactor shell, and described jet-flow aeration three-phase homogeneous plate is horizontally disposed with.
On described jet-flow aeration three-phase homogeneous plate, the porosity of micropore is 0.0001-0.1; Described micropore is uniformly distributed on described jet-flow aeration three-phase homogeneous plate, and the spacing of every adjacent two micropores is 100-10000 micron.
The aperture of each described micropore first reduces gradually along the flow direction of slurry, then increases gradually, and the minimum-value aperture of each described micropore is greater than or equal to 50 microns, and maximum diameter of hole is less than or equal to 1000 microns.
On the sidewall of described reactor shell, be provided with cold hydrogen injection device and cold oil injection device.
Described cold hydrogen injection device and cold oil injection device are respectively arranged with multiple, and wherein each described cold oil injection device in the vertical direction is between two described cold hydrogen injection devices.
Described cold hydrogen injection device comprises:
Snorkel, described snorkel runs through the sidewall setting of described reactor shell;
Plate-like gas distribution pipe, is connected setting with the outlet side of described snorkel, on described plate-like gas distribution pipe, is provided with venthole, the transverse cross-section parallel setting of described plate-like gas distribution pipe and described reactor shell.
The oil-out of described cold oil injection device is arranged on the axis of described reactor shell and in axial direction and arranges downwards.
Based on the hydrogenation technique of described jet-flow aeration three-phase homogeneous reactor, comprise the following steps: feedstock oil is mixed with hydrogenation catalyst, and then after mixing with hydrogen, slurry intake channel from described jet-flow aeration three-phase homogeneous reactor bottom is sent into reactor, and the three-phase uniform homogeneous blend flowing out from described jet three-phase homogeneous plate micropore is 0.5h in liquid hourly space velocity (LHSV)
-1, hydrogen dividing potential drop 20MPa, reaction temperature be to carry out hydrogenation reaction under 450 DEG C of conditions.
The cold hydrogen injection device arranging on sidewall by described reactor shell and cold oil injection device inject, and are that the heavy oil of the hydrogen of 30-50 DEG C and/or 30-80 DEG C is to ensure that reaction temperature is as 300-500 DEG C to implantation temperature in described jet-flow aeration three-phase homogeneous reactor.
Described hydrogenation catalyst comprises carrier and be carried on the active metal component on described carrier, and wherein said carrier is graphitization reaming Carbon Materials, and the specific area of described graphitization reaming Carbon Materials is 200-600m
2/ g, average pore size is 10-100nm, pore volume is 0.3-1.0cm
3/ g, described carrier accounts for the 70wt%-98wt% of described hydrogenation catalyst gross mass.
Based on the hydrogenation technique of jet-flow aeration three-phase homogeneous reactor described in the utility model, feedstock oil is mixed with hydrogenation catalyst, and then after mixing with hydrogen, slurry intake channel from described jet-flow aeration three-phase homogeneous reactor bottom is sent into reactor, and the three-phase uniform homogeneous blend flowing out from described jet three-phase homogeneous plate micropore is 0.1-4.0/h in liquid hourly space velocity (LHSV)
-1, hydrogen dividing potential drop is that 10-30MPa, reaction temperature are, under the condition of 300-500 DEG C, to carry out hydrogenation reaction, under this reaction condition, in heavy oil, the conversion ratio of 500 DEG C of above cuts of conventional boiling point is the highest.As preferred embodiment, the utility model is that the heavy oil of the hydrogen of 30-50 DEG C and/or 30-80 DEG C is to ensure that reaction temperature is as 300-500 DEG C by cold hydrogen injection device and cold oil injection device to implantation temperature in described jet-flow aeration three-phase homogeneous reactor.
Hydrogenation catalyst described in the utility model comprises carrier and be carried on the active metal component on described carrier, and wherein, described carrier is graphitization reaming Carbon Materials, and the specific area of described graphitization reaming Carbon Materials is 200-600m
2/ g, average pore size is 10-100nm, pore volume is 0.3-1.0cm
3/ g, described carrier accounts for the 70wt%-98wt% of described hydrogenation catalyst gross mass.Wherein said carrier is graphitization reaming Carbon Materials, described graphitization reaming Carbon Materials is that the carbon feedstock of pulverizing is carried out after graphitization processing under 1500-1900 DEG C of condition, recycling staving press carries out reaming processing and makes, and the time of wherein said graphitization processing is 0.5-8.0h; The specific area of graphitization reaming Carbon Materials is 200-960m
2/ g, average pore size is 10-100nm, pore volume is 0.3-1.0cm
3/ g, described carrier accounts for the 70wt%-98wt% of described hydrogenation catalyst gross mass.Hydrogenation catalyst described in the utility model, the effect of the large π key of the layer structure of graphite and conjugation delocalized electron in graphitized carbon material support, make carrier surface there is stronger alkalescence and electric conductivity, the formation of the large π key of conjugation is easy to receive and discharge the free radical electronics of storage, thereby after generate longer-chain hydrocarbons fracture, Stable Carbon free radical, the delayed coking time, be beneficial to and make it react the required product of generation with hydroperoxyl radical, avoid the direct coking of carbon radicals to form collection charcoal on the surface of catalyst, promote the removal to metal impurities in feedstock oil, improve the activity of catalyst, and then raising feedstock oil conversion ratio and liquid yield.As further preferred embodiment, the particle diameter of described hydrogenation catalyst is 1-7 μ m, and described active metal component comprises one or more in group VIII metal oxide and group vib metal oxide.
Technique scheme of the present utility model has the following advantages compared to existing technology:
(1) jet-flow aeration three-phase homogeneous reactor described in the utility model, it is by described reactor shell bottom or jet-flow aeration three-phase homogeneous plate is set in slurry intake channel, and on described jet-flow aeration three-phase homogeneous plate, be provided with and connect the micropore of described jet-flow aeration three-phase homogeneous plate, thereby by oil product, the three-phase mixture of hydrogen and catalyst is flowed through after described micropore, make the bubble of gas and the drop of liquid become tiny and even, and then tiny, the bubble of homogenising and drop will more be conducive to above-mentioned gas, liquid, Gu the phase counterdiffusion between three-phase material with fully contact, exist when make-up gas distributor is set and cannot realize gas compared to three phase slurry bed bioreactor in prior art, liquid, Gu the full and uniform mixing of three-phase, the problem that reaction efficiency is low, jet-flow aeration three-phase homogeneous reactor described in the utility model can be realized oil product, the full and uniform mixing of hydrogen and catalyst three-phase, thereby be that oil product and hydrogen react the sufficient touch opportunity of creation on catalyst surface, make reaction more abundant, reaction efficiency is high.
(2) jet-flow aeration three-phase homogeneous reactor described in the utility model, wherein said jet-flow aeration three-phase homogeneous plate is arranged in the slurry intake channel of described reactor shell bottom, thereby the charging that is conducive to enter from bottom reactor is able to abundant mixing, and then ensure the maximization of reactor utilization ratio.
(3) jet-flow aeration three-phase homogeneous reactor described in the utility model, the aperture that each described micropore is set first reduces gradually along the flow direction of slurry, increase gradually again, the advantage arranging is like this: the flow through process in aperture from large to small of slurry, be the process that flow rate of slurry increases gradually, known according to Bernoulli equation, now the static energy of fluid changes to kinetic energy, in the time flowing through the minimum place in aperture, the flow velocity of slurry is the fastest, pressure minimum, now the light-end products in slurry will be vaporized into because of the reduction of pressure minute bubbles; Then, slurry becomes large flow process from aperture is minimum gradually to aperture, is above-described inverse process, and now, the minute bubbles of vaporization are because the rising of pressure can be broken rapidly; The structure that micropore size first reduces gradually, increases gradually belongs to good stream shape, reduce to greatest extent the flow through pressure drop of jet-flow aeration three-phase homogeneous plate of fluid, therefore, whole process has completed hydrogen and has been dissolved in rapidly the process of oil product, has also promoted the even mixing of catalyst granules and oil product simultaneously.
(4) jet-flow aeration three-phase homogeneous reactor described in the utility model, wherein the minimum-value aperture of each described micropore is greater than or equal to 50 microns, maximum diameter of hole is less than or equal to 1000 microns, on the one hand, the minimum diameter of described micropore is greater than 5 times (catalyst granules diameter is 5-10 micron) of the maximum particle diameter of catalyst, thereby ensures that catalyst granules can not stop up when by micropore; On the other hand, the diameter of described micropore is less, is preferably no more than 1000 microns, make the bubble diameter of formation less, capillary effect is stronger, forms bubble just easier, the time that bubble maintains in uphill process is just longer, is conducive to the uniform and stable property of whole system.
(5) jet-flow aeration three-phase homogeneous reactor described in the utility model, on the sidewall of described reactor shell, be provided with cold hydrogen injection device and cold oil injection device, on the one hand, the injection of cold medium can ensure that oil product can not cause the gasification of light-end products and the huge change of liquid phase oil property in the reactor that causes in the process of lighting, make reactor all the time in mitigation state, be easier to operation; On the other hand, by injecting cold medium on the sidewall at jet-flow aeration three-phase homogeneous reactor, instead of inject from the bottom inlet of jet-flow aeration three-phase homogeneous bed bioreactor, can ensure reactor temperature relatively constant in the axial direction, can be all the time in best reaction temperature.As preferred embodiment, the utility model described cold hydrogen injection device of restriction and cold oil injection device are respectively arranged with multiple, and wherein each described cold oil injection device in the vertical direction is between two described cold hydrogen injection devices.Its reason is: whole reaction is carried out in the axial direction from bottom to top gradually, the variation of the interior state of reactor is also mainly because chemical reaction causes, thus the above-mentioned stability that can ensure to greatest extent the reactivenesses such as reactor interior reaction temperature, fluid density, catalyst concn that arranges.And, as further preferred embodiment, the aspirating end that the utility model also limits described cold hydrogen injection device is plate-like gas distribution pipe, the oil-out of described cold oil injection device is arranged on the axis of described reactor shell and in axial direction and arranges downwards, this is because be mainly liquid phase in reactor, liquid phase is continuous phase, after cold hydrogen injecting reactor, be that the form that is bubble moves upward continuously, self can complete the axially upper uniformity distributing, so it is uniform substantially that bubble distributes in the axial direction, and ensure that the uniformity that bubble distributes diametrically just need to arrange distributed component at decanting point section, and for the decanting point of cold oil, because the cold oil injecting is poor less with the oil density in reactor, substantially can not produce relative motion, just can automatically not complete the uniformity that cold oil distributes in the axial direction yet, so want to solve the uniformity distributing on reactor is axial, the oil-out that cold oil injection device just need to be set arranges downwards on reactor axis and in axial direction.
Brief description of the drawings
For content of the present utility model is more likely to be clearly understood, below in conjunction with accompanying drawing, the utility model is described in further detail, wherein,
Fig. 1 is the structural representation of jet-flow aeration three-phase homogeneous reactor described in the utility model embodiment 1;
Fig. 2 is the structural representation of jet-flow aeration three-phase homogeneous reactor described in the utility model embodiment 2;
Fig. 3 is the schematic diagram of part microcellular structure on jet-flow aeration homogeneous plate described in the utility model;
Fig. 4 is the generalized section of microcellular structure described in the utility model.
In figure, Reference numeral is expressed as: 1-reactor shell, 11-slurry intake channel, 12-discharging channel, 2-jet-flow aeration homogeneous plate, 21-micropore, the cold hydrogen injection device of 3-, 4-cold oil injection device.
Detailed description of the invention
Embodiment 1
The present embodiment provides a kind of jet-flow aeration three-phase homogeneous reactor, and its structure as shown in Figure 1, comprising:
Reactor shell 1, is connected with slurry intake channel 11 with the bottom of described reactor shell, is connected with discharging channel 12 with the top of described reactor shell;
Jet-flow aeration three-phase homogeneous plate 2, described jet-flow aeration three-phase homogeneous plate is horizontally set in described reactor shell and is positioned at the bottom of described reactor shell, as shown in Figure 3 and Figure 4, on described jet-flow aeration three-phase homogeneous plate 2, be evenly arranged micropore 21, described micropore runs through the setting of described jet-flow aeration three-phase homogeneous plate; As the embodiment that can select, on described jet-flow aeration three-phase homogeneous plate, the porosity of micropore is 0.0001-0.1, the spacing of every adjacent two micropores is 100-10000 micron, as preferred embodiment, porosity described in the present embodiment is 0.00029,2600 microns of the spacing of every adjacent two micropores; The aperture of described micropore first reduces gradually along the flow direction of slurry, increase gradually, wherein the maximum diameter of hole of each micropore is 1000 microns again, and minimum-value aperture is 50 microns, as preferred embodiment, the minimum-value aperture place of micropore described in the present embodiment is positioned at the centre position of described micropore;
Cold hydrogen injection device 3 and cold oil injection device 4, as the embodiment that can select, on the sidewall of described reactor shell 1, set gradually four described cold hydrogen injection devices and two cold oil injection devices, described four cold hydrogen injection devices vertically, be arranged in order from top to bottom, and two cold oil injection devices are also vertically to arrange from top to bottom, on one of them cold oil injection device, be arranged on from top to bottom between several first and second cold hydrogen injection devices, another is arranged between third and fourth cold hydrogen injection device; As preferred embodiment, described cold hydrogen injection device 3 includes snorkel and plate-like gas distribution pipe, described snorkel runs through the sidewall setting of described reactor shell, described plate-like gas distribution pipe is connected setting the transverse cross-section parallel with described reactor shell with the outlet side of described snorkel, on described plate-like gas distribution pipe, be provided with venthole; Preferably, the oil-out of described cold oil injection device 4 is all arranged on the axis of described reactor shell and in axial direction and arranges downwards.
Described in the present embodiment, jet-flow aeration three-phase homogeneous reactor is in the time carrying out heavy-oil hydrogenation processing, and its technological process is as follows:
Coal tar is mixed in head tank by measuring pump according to the ratio of weight ratio 100:0.1 with hydrogenation catalyst and stir after boost to 25MPa by High pressure feeding pump, then with the hydrogen of uniform pressure in mass ratio the ratio of 12:1 mix, make its slurry intake channel 11 from described reactor shell 1 bottom enter reactor, described slurries, by from bottom to top by the micropore 21 of jet-flow aeration three-phase homogeneous plate 2, are realized the abundant mixing of three-phase afterwards.The three-phase uniform homogeneous blend flowing out from jet three-phase homogeneous plate micropore is 0.5h in liquid hourly space velocity (LHSV)
-1, hydrogen dividing potential drop 20MPa, reaction temperature be under 450 DEG C of conditions, in jet-flow aeration three-phase homogeneous reactor, contact fully and react.But because hydrogenation reaction is exothermic reaction, reactor is again adiabatic reactor, reaction liberated heat will be absorbed by self and cause the temperature of medium self to raise, now by described cold hydrogen injection device 3 and cold oil injection device 4 implantation temperatures be the cold hydrogen of 40 DEG C and temperature be the cold oil of 60 DEG C will reaction after the reduction of medium temperature, thereby ensure that reactor is all the time in best reactiveness.Wherein, the gross mass of injecting cold oil accounts for 30% of feedstock oil gross mass, and the gross mass of injecting cold hydrogen accounts for 6.7% of feedstock oil gross mass.After having reacted, product is discharged from the discharging channel 12 of reactor head, delivers to product separation system and isolates dry gas, naphtha, diesel oil, wax oil and residue.
Further, because jet-flow aeration three-phase homogeneous plate described in the present embodiment is arranged on the bottom of reactor shell, and micropore percent opening and diameter on jet-flow aeration three-phase homogeneous plate are all very little, in the time of reactor down-time, need to be by more than jet-flow aeration three-phase homogeneous plate in reactor drawing off containing solid-liquid.As the embodiment that can select, reactor described in the present embodiment, can in jet-flow aeration three-phase homogeneous plate upper portion side wall, discharge gate be set, in the time that reactor down-time is carried out discharging, the material that is positioned at described jet-flow aeration three-phase homogeneous plate top is discharged by described discharge gate.
Hydrogenation catalyst described in the present embodiment comprises carrier and be carried on the active metal component on described carrier, and wherein said carrier is graphitization reaming Carbon Materials, and the specific area of described graphitization reaming Carbon Materials is 200m
2/ g, average pore size is 38nm, pore volume is 0.3cm
3/ g, described carrier accounts for the 70wt% of described hydrogenation catalyst gross mass.Described active metal component is the oxide of iron, and the oxide of described iron is (with Fe
2o
3meter) account for the 30.0wt% of described hydrogenation catalyst agent content.The preparation method of described hydrogenation catalyst is: blue carbon feedstock is pulverized, crossed 280 mesh sieves, after 120 DEG C of oven dry dewater, be placed in high temperature furnace, under inert gas shielding, in 1500 DEG C of processing 8.0h, when equitemperature drops to room temperature, take out; By after the graphitized carbon material of graphitization processing and KOH expanding agent are dry mixed evenly with the amount of mass ratio 1:2, be placed in the tube furnace of oxygen and nitrogen (volume ratio 1:9) mixed atmosphere, at 500 DEG C, carry out reaming and process 0.5h; Reaming sample is after pickling, washing, and centrifugation, in 100 DEG C of dry 3h, obtains the blue charcoal carrier of graphitization reaming; Take 150gFeSO
47H
2o, as active component predecessor, adopts equi-volume impregnating to be impregnated on the blue charcoal of the above-mentioned graphitization reaming of 100g, after dipping, at 120 DEG C of dry 6h, then through ball milling 4h, obtains the hydrogenation catalyst that particle diameter is 1-7 μ m.
Embodiment 2
Jet-flow aeration three-phase homogeneous reactor described in the present embodiment, its structure as shown in Figure 2, comprising:
Reactor shell 1, is connected with slurry intake channel 11 with the bottom of described reactor shell, is connected with discharging channel 12 with the top of described reactor shell;
Jet-flow aeration three-phase homogeneous plate 2, described jet-flow aeration three-phase homogeneous plate is arranged in described slurry intake channel, and with the transverse cross-section parallel of described slurry intake channel 11; On described jet-flow aeration three-phase homogeneous plate 2, be evenly arranged micropore 21, described micropore runs through the setting of described jet-flow aeration three-phase homogeneous plate; As the embodiment that can select, on described jet-flow aeration three-phase homogeneous plate, the porosity of micropore is 0.0001-0.1, and the spacing of every adjacent two micropores is 100-10000 micron, preferably, porosity described in the present embodiment is 0.006, and the spacing of every adjacent two micropores is 560 microns; The aperture of described micropore 21 first reduces gradually along the flow direction of slurry, increase gradually again, wherein the maximum diameter of hole of each described micropore is 750 microns, minimum-value aperture is 150 microns, as preferred embodiment, the minimum-value aperture place of micropore described in the present embodiment is positioned at the centre position of described micropore;
Cold hydrogen injection device 3 and cold oil injection device 4, as the embodiment that can select, on the sidewall of described reactor shell 1, set gradually four described cold hydrogen injection devices and two cold oil injection devices, described four cold hydrogen injection devices vertically, be arranged in order from top to bottom, and two cold oil injection devices are also vertically to arrange from top to bottom, on one of them cold oil injection device, be arranged on from top to bottom between several first and second cold hydrogen injection devices, another is arranged between third and fourth cold hydrogen injection device; As preferred embodiment, each described cold hydrogen injection device 3 includes snorkel and plate-like gas distribution pipe, described snorkel runs through the sidewall setting of described reactor shell, described plate-like gas distribution pipe is connected setting the transverse cross-section parallel with described reactor shell with the outlet side of described snorkel, on described plate-like gas distribution pipe, be provided with venthole; Preferably, the oil-out of each described cold oil injection device 4 is all arranged on the axis of described reactor shell and in axial direction and arranges downwards.
Because jet-flow aeration three-phase homogeneous plate described in the present embodiment is arranged in slurry intake channel, as the embodiment that can select, can on the feeding-passage of jet-flow aeration three-phase homogeneous plate top, discharge gate be set, in the time that reactor down-time is carried out discharging, the material in reactor can directly be discharged by the discharge gate on described slurry intake channel again.Described in the present embodiment, jet-flow aeration three-phase homogeneous reactor is in the time carrying out heavy-oil hydrogenation processing, and its technological process is as follows:
Residual oil is mixed in head tank by measuring pump according to the ratio of weight ratio 100:0.1 with hydrogenation catalyst and stir after boost to 25MPa by High pressure feeding pump, then with the hydrogen of uniform pressure in mass ratio the ratio of 12:1 mix, make its slurry intake channel 11 from described reactor shell 1 bottom enter reactor, described slurries, by from bottom to top by the micropore 21 of jet-flow aeration three-phase homogeneous plate 2, are realized the abundant mixing of three-phase afterwards.The three-phase uniform homogeneous blend flowing out from jet three-phase homogeneous plate micropore is 0.5h in liquid hourly space velocity (LHSV)
-1, hydrogen dividing potential drop 20MPa, reaction temperature be under 450 DEG C of conditions, in jet-flow aeration three-phase homogeneous reactor, contact fully and react.But because hydrogenation reaction is exothermic reaction, reactor is again adiabatic reactor, reaction liberated heat will be absorbed by self and cause the temperature of medium self to raise, now by described cold hydrogen injection device 3 and cold oil injection device 4 implantation temperatures be the cold hydrogen of 40 DEG C and temperature be the cold oil of 60 DEG C will reaction after the reduction of medium temperature, thereby ensure that reactor is all the time in best reactiveness.Wherein, the gross mass of injecting cold oil accounts for 30% of feedstock oil gross mass, and the gross mass of injecting cold hydrogen accounts for 6.7% of feedstock oil gross mass.After having reacted, product is discharged from the discharging channel 12 of reactor head, delivers to product separation system and isolates dry gas, naphtha, diesel oil, wax oil and residue.
Hydrogenation catalyst described in the present embodiment, comprises carrier and is carried on the active metal component on described carrier, wherein said carrier is graphitization reaming Carbon Materials, and the specific area of described graphitization reaming Carbon Materials is 960m
2/ g, average pore size is 100nm, pore volume is 1.0cm
3/ g, described carrier accounts for the 98wt% of described hydrogenation catalyst gross mass.Active metal component described in the present embodiment is cobalt oxide, and described cobalt oxide accounts for 2.0% of described hydrogenation catalyst gross mass.The preparation method of the hydrogenation catalyst described in the present embodiment is: active carbon raw material is pulverized, crossed 280 mesh sieves, after 120 DEG C of oven dry dewater, be placed in high temperature furnace, under inert gas shielding, in 1800 DEG C of processing 5h, when equitemperature drops to room temperature, take out; After the expanding agent forming through the graphitization absorbent charcoal material of graphitization processing and KOH and NaOH mixture (mass ratio 1:1) is dry mixed evenly with the amount of mass ratio 1:6, be placed in the tube furnace of air atmosphere, at 1000 DEG C, carry out reaming and process 8h; Reaming sample is after pickling, washing, and centrifugation, in 100 DEG C of dry 3h, obtains graphitization reaming activity carbon carrier; Take 7.64gCoSO
47H
2o, as active component predecessor, adopts equi-volume impregnating to be impregnated on the above-mentioned graphitization reaming of 100g active carbon, after dipping, at 120 DEG C of dry 6h, then through ball milling 6h, obtains the hydrogenation catalyst that particle diameter is 1-7 μ m.
In above-described embodiment 1 and 2, specific surface and the pore structure of the blue carbon carrier of described graphitization reaming are tested on the ASAP2020 instrument of Micrometrics company of the U.S., specific surface calculates according to Berrett-Emmett-Teller (BET) method, and pore volume and pore-size distribution prop up according to Berret-Joyner-Halenda (BJH) model and calculate according to desorption.
Feedstock oil conversion ratio (520 DEG C of following constituent masses (containing gas)/feedstock oil quality × 100%), distillate yield (520 DEG C of following liquid component quality/feedstock oil quality × 100%) and metal removal rate ((1-generates the tenor in the tenor/raw material in oil) × 100%) to the hydroprocessing technique in the utility model embodiment 1 and 2 are tested, find that the feedstock oil conversion ratio in embodiment 1 and 2 is greater than 81%, distillate yield is greater than 69%, and metal removal rate is greater than 93%.
Obviously, above-described embodiment is only for example is clearly described, and the not restriction to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here without also giving exhaustive to all embodiments.And among the protection domain that the apparent variation of being extended out thus or variation are still created in the utility model.
Claims (9)
1. a jet-flow aeration three-phase homogeneous reactor, comprising:
Reactor shell, is connected with slurry intake channel with the bottom of described reactor shell, is connected with discharging channel with the top of described reactor shell;
It is characterized in that,
In described reactor shell and be positioned at the bottom of described reactor shell, or in described slurry intake channel, be provided with jet-flow aeration three-phase homogeneous plate, on described jet-flow aeration three-phase homogeneous plate, be furnished with micropore, described micropore runs through the setting of described jet-flow aeration three-phase homogeneous plate.
2. jet-flow aeration three-phase homogeneous reactor according to claim 1, is characterized in that, described jet-flow aeration three-phase homogeneous plate is arranged in described slurry intake channel, the transverse cross-section parallel setting of described jet-flow aeration three-phase homogeneous plate and described slurry intake channel.
3. jet-flow aeration three-phase homogeneous reactor according to claim 1, is characterized in that, described jet-flow aeration three-phase homogeneous plate is arranged in described reactor shell and is positioned at the bottom of described reactor shell, and described jet-flow aeration three-phase homogeneous plate is horizontally disposed with.
4. according to the arbitrary described jet-flow aeration three-phase homogeneous reactor of claim 1-3, it is characterized in that, on described jet-flow aeration three-phase homogeneous plate, the porosity of micropore is 0.0001-0.1; Described micropore is uniformly distributed on described jet-flow aeration three-phase homogeneous plate, and the spacing of every adjacent two micropores is 100-10000 micron.
5. jet-flow aeration three-phase homogeneous reactor according to claim 4, it is characterized in that, the aperture of each described micropore first reduces gradually along the flow direction of slurry, increase gradually again, the minimum-value aperture of each described micropore is greater than or equal to 50 microns, and maximum diameter of hole is less than or equal to 1000 microns.
6. according to the jet-flow aeration three-phase homogeneous reactor described in claim 1 or 2 or 3 or 5, it is characterized in that, on the sidewall of described reactor shell, be provided with cold hydrogen injection device and cold oil injection device.
7. jet-flow aeration three-phase homogeneous reactor according to claim 6, it is characterized in that, described cold hydrogen injection device and cold oil injection device are respectively arranged with multiple, and wherein each described cold oil injection device in the vertical direction is between two described cold hydrogen injection devices.
8. jet-flow aeration three-phase homogeneous reactor according to claim 6, is characterized in that, described cold hydrogen injection device comprises:
Snorkel, described snorkel runs through the sidewall setting of described reactor shell;
Plate-like gas distribution pipe, is connected setting with the outlet side of described snorkel, on described plate-like gas distribution pipe, is provided with venthole, the transverse cross-section parallel setting of described plate-like gas distribution pipe and described reactor shell.
9. jet-flow aeration three-phase homogeneous reactor according to claim 6, is characterized in that, the oil-out of described cold oil injection device is arranged on the axis of described reactor shell and in axial direction and arranges downwards.
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| CN201420093569.2U CN203750518U (en) | 2014-03-03 | 2014-03-03 | Fluidic aeration three-phase homogeneous reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861532A (en) * | 2014-03-03 | 2014-06-18 | 北京旭荣工程设计有限公司 | Homogeneous three-phase reactor for jet aeration |
| CN108548817A (en) * | 2018-03-26 | 2018-09-18 | 清华大学 | Multiphase bouyant jet tests generating means and oil droplet bubble shadow image processing method |
-
2014
- 2014-03-03 CN CN201420093569.2U patent/CN203750518U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861532A (en) * | 2014-03-03 | 2014-06-18 | 北京旭荣工程设计有限公司 | Homogeneous three-phase reactor for jet aeration |
| CN103861532B (en) * | 2014-03-03 | 2015-11-18 | 北京华石联合能源科技发展有限公司 | A kind of jet-flow aeration three-phase homogeneous reactor |
| CN108548817A (en) * | 2018-03-26 | 2018-09-18 | 清华大学 | Multiphase bouyant jet tests generating means and oil droplet bubble shadow image processing method |
| CN108548817B (en) * | 2018-03-26 | 2021-08-03 | 清华大学 | Multiphase floating jet experiment generating device and oil drop bubble shadow image processing method |
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