CN208145916U - The exhaust system of liquid phase hydrogenation reactor - Google Patents
The exhaust system of liquid phase hydrogenation reactor Download PDFInfo
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- CN208145916U CN208145916U CN201820207999.0U CN201820207999U CN208145916U CN 208145916 U CN208145916 U CN 208145916U CN 201820207999 U CN201820207999 U CN 201820207999U CN 208145916 U CN208145916 U CN 208145916U
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- 239000007791 liquid phase Substances 0.000 title claims abstract description 60
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 72
- 238000000926 separation method Methods 0.000 claims abstract description 40
- 230000005540 biological transmission Effects 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 230000004888 barrier function Effects 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 4
- 239000000945 filler Substances 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims 1
- 239000012495 reaction gas Substances 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 abstract description 37
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 37
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 32
- 230000000694 effects Effects 0.000 abstract description 5
- 150000002431 hydrogen Chemical class 0.000 abstract description 5
- 238000004090 dissolution Methods 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 21
- 239000010410 layer Substances 0.000 description 20
- 238000000034 method Methods 0.000 description 19
- 239000000463 material Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- 239000006227 byproduct Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000003350 kerosene Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000006254 arylation reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- -1 distillate Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000002184 metal Substances 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
- 230000036961 partial effect Effects 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000009790 rate-determining step (RDS) Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Abstract
The utility model is a kind of exhaust system of liquid phase hydrogenation reactor.The exhaust system of the liquid phase hydrogenation reactor of the utility model includes the gas-liquid separation component outside gas deflation assembly and reactor in reactor end socket, and gas vent is arranged in reactor head, and gas vent is connect by gas transmission line with gas-liquid separation component；The gas deflation assembly includes distribution grid, several groups liter inflator and liquid-blocking cap；Every group of liter inflator and liquid-blocking cap are evenly arranged in distribution plate surface, and liquid-blocking cap is connect by gusset with inflator top is risen.The phenomenon that exhaust system is conducive to increase oil product to the mixed dissolution of hydrogen, reduces and discharges gas evolution, while can effectively reduce discharge gas carrying liquid generation, improves hydrodesulfurization effect, reduces hydrogen consumption.
Description
Technical field
The utility model relates to a kind of exhaust system of liquid phase hydrogenation reactor, the liquid phase for being particularly suitable for virgin kerosene adds
Hydrogen refining reaction.
Background technique
Liquid-phase hydrogenatin technique is a kind of novel, efficient, low energy consumption hydrogen addition technology, with conventional trickle bed hydrogenation technique phase
Than having the advantage that：（1）The influence of hydrogen mass transfer can be eliminated.This is mainly due in trickle bed hydrogenation technique, hydrogen from
Gas phase diffusion is simultaneously dissolved into the rate-determining steps that the speed in oil is entire hydrogenation reaction, and liquid-phase hydrogenatin technique makes hydrogenation reaction exist
Dynamics Controlling area carries out, i.e., hydrogen is dissolved in feedstock oil to meet hydrogen needed for hydrogenation reaction, makes hydrogenation reaction pure
It is carried out in liquid phase, eliminating mass transfer of the hydrogen from gas phase to liquid phase influences；（2）Hydrocarbon oil hydrogenation process actually participates in the hydrogen of reaction
Only for the hydrogen of chemical hydrogen consumption, and traditional trickle bed reactor hydrogen addition technology, needing excessive hydrogen exists, and makes
The volume for obtaining reactor is bigger, and hydrogen is then dissolved in feedstock oil by liquid-phase hydrogenatin process, therefore reactor and reaction system
System volume can significantly reduce；（3）Compared with traditional drip bed process, liquid-phase hydrogenatin process requirement remains a large amount of superfluous
Hydrogen, thus need to use circulating hydrogen compressor, it is not provided with complicated circulation hydrogen system in liquid-phase hydrogenatin process flow, can save
The investment of the equipment such as circulating hydrogen compressor and high-pressure separator.And in liquid-phase hydrogenatin technique, hydrodesulfurization by-product H2S is to adding
Hydrogen desulfurization, denitrogenation, de- arylation reaction also have apparent inhibiting effect, a small amount of H2S, which exists, just will be greatly reduced hydrodesulfurization rate, and
And H2S is adsorbed as monolayer adsorption catalyst surface, once adsorption site is by H2S is occupied, and reaction rate will be no longer with H2S points
Pressure improves and declines, therefore liquid-phase hydrogenatin needs interruption is outer 2 S component is discharged, and eliminates H2The influence of S, is just able to achieve depth
Desulfurization.
In existing liquid-phase hydrogenatin technique, the general mode for taking interruption or continuous exhaust pneumatic wallop at the top of liquid phase hydrogenation reactor, one
Aspect controls reactor head pressure, and on the other hand discharge contains H2The gas of S, and during gas discharging, generally
Using conventional simple exhaust outlet and exhaust system, reaction system fluctuation etc. when there is large-minded discharge, discharge gas carrying liquid, exhaust
Problem, and existing patent has focused largely on liquid-phase hydrogenatin technique, reaction raw materials oil mixes hydrogen, inside reactor mixes hydrogen etc.,
It is less to the report of reactor exhaust aspect.
CN102358847A proposes a kind of method of full liquid-phase hydrogenatin process for producing cleaning diesel oil, and this method includes：It is former
Material, hydrogen and circulating liquid hydrogenation products carry out hydrogen saturation in pipeline, form a kind of raw material/hydrogenation products/hydrogen liquid phase
Mixture is saturated the liquid phase mixture segmentation of dissolved hydrogen into multistage conventional hydro reactor under hydrogenation process conditions, and from
Reactor head discharge contains by-product H2S、NH3Oil gas.This method has hydrogenator and simultaneously by by-product H2S、
NH3The function of discharge.But contain by-product H in the hydrogenator2S、NH3Exhaust of oil mouth and exhaust system be it is conventional,
That there are capacities is big, discharge gas carrying liquid, exhaust when reactor operation fluctuation the problems such as.
Summary of the invention
In view of the deficiencies of the prior art, the utility model provides a kind of exhaust system of liquid phase hydrogenation reactor.The exhaust
System is conducive to increase oil product to the mixed dissolution of hydrogen, reduction discharge gas evolution, while can effectively reduce discharge gas carrying liquid
The phenomenon that occur, improve hydrodesulfurization effect, reduce hydrogen consumption.
The exhaust system of the liquid phase hydrogenation reactor of the utility model includes gas deflation assembly and reaction in reactor end socket
Gas vent is arranged in gas-liquid separation component outside device, reactor head, and gas vent passes through gas transmission line and gas-liquid separation component
Connection；The gas deflation assembly includes distribution grid, several groups liter inflator and liquid-blocking cap；Every group of liter inflator and liquid-blocking cap are in distribution grid
Surface is evenly arranged, and liquid-blocking cap is connect by gusset with inflator top is risen.
The distribution grid of the gas deflation assembly is the sieve-plate structure of surface uniform pore openings, seals and connect with hydrogenator inner wall
It connects.
The liter inflator of the gas deflation assembly is welded on distribution grid；Rise air cylinder body be partially immersed in reactor liquid level with
Under, it is preferably submerged in 1/4 ~ 1/2 that subsurface part is cylinder total height.
Gas-liquid separation component described in the utility model can be the structure of gas liquid separator of conventional well known, as gravity is heavy
Any one in drop, baffling separation, centrifuge separation, silk screen separation, filler separated structure etc..It is preferred that using the gas of following structures
Liquid separation assembly, the gas-liquid separation component include cylindrical drum and back taper bottom, setting row at the top of gas-liquid separation component
Leakage fluid dram is arranged in port, back taper bottom, and leakage fluid dram is connected to through liquid reflux pipeline with liquid phase in reactor.
Further, 2N layers of baffling component, every layer of baffling group are set from the bottom to top in the drum shape cylinder body of gas-liquid separation component
Part includes several profiled baffle plates, wherein N >=1, and the upper limit of N is determined according to reaction actual needs, N preferably 2 ~ 4.Profiled baffle plate
It is spliced including three pieces of hydraulic barriers, first piece is inclined plate with third block, and second block of level board, second piece of both ends connect respectively
Connect first piece and third block, three pieces of baffle groups concavities or convex structure；It is preferred that the profiled baffle plate in every layer of baffling component
For identical structure；Profiled baffle plate in more preferably adjacent odd-level and even level is staggered, further preferably adjacent
Odd-level and even level in, the profiled baffle plate of odd-level is concave structure, and the profiled baffle plate of even level is convex structure.
Gas-liquid separation component purpose described in the utility model is to send out gas can under the action of profiled baffle plate
Raw multiple baffling and change direction avoid occurring the phenomenon that gas short circuit occurs, enhances gas-liquid separation effect, reduces gas carrying liquid.
The utility model provides a kind of liquid phase hydrogenation reactor using above-mentioned exhaust system simultaneously, and the liquid phase adds
Hydrogen reactor further includes inlet diffuser, catalyst bed and liquid distribution trough.
In the utility model, is at least realized in liquid phase hydrogenation reactor and remove its sulphur, nitrogen, oxygen, a kind of dirt in metal impurities
Object is contaminated, and is saturated aromatic hydrocarbons, changes hydrocarbonaceous oil molecules structure.
In the utility model, the inlet diffuser of liquid phase hydrogenation reactor is set at material inlet, for react into
Material carries out rectification distribution and throttling buffering.
In the utility model, the liquid phase hydrogenation reactor is used for hydrodesulfurization, the hydrodenitrogeneration, hydrogenation dearomatization of hydrocarbon ils
Hydrocarbon purification；The fresh feed oil used can be hydrocarbon ils or distillate, as petroleum distillate, distillate, diesel oil, deasphalted oil,
Residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
In the utility model, the operating condition of liquid phase hydrogenation reactor is：Reaction temperature is 150~450 DEG C, fresh feed
Volume space velocity is 0.5h-1~6.0h-1, hydrogen partial pressure is 2.0~10MPa.
The course of work of the liquid phase hydrogenation reactor of the utility model is as follows：Raw material initially enters hydrogenator, is entering
After mouth diffuser and liquid distribution trough progress material are uniformly distributed, liquid-phase hydrogenatin reaction, reaction effluent occurs into catalyst bed
It is left via discharge port；During the reaction, it can use exhaust system of the mode continuously or discontinuously by reactor head
Discharge contains by-product H2S、NH3Oil gas, discharge air cooling lime set by liquid return tube is back to reactor.
The utility model has the following advantages that：The exhaust of this exhaust system is more uniform, escapes under liquid level in reactor
Gas from liquid-blocking cap and rise the gap between inflator and flow out, emergent gas on the other hand may be made again by the limitation of the slit
It is secondary to be dissolved in feedstock oil, emergent gas amount is reduced, the consumption of hydrogen is reduced；On-line continuous discharge may be implemented and contain by-product
H2S、NH3Oil gas, be advantageously implemented deep desulfuration；Reduce the generation of gas carrying liquid phenomenon, the operating process for discharging on-line continuous
Become sufficiently stable, when continuous small volume exhaust operation, the loss of hydrogen less, material consumption it is lower, economy is more preferable.
Detailed description of the invention
Fig. 1 is the liquid phase hydrogenation reactor and structural schematic diagram of the utility model.
Fig. 2 is the exhaust system structure schematic diagram of the utility model.
Wherein：1- liquid phase hydrogenation reactor；2- inlet diffuser；3- catalyst bed；4- exhaust system；5- exhaust outlet；
4-1- gas deflation assembly；4-2- distribution grid；4-3- rises inflator；4-4- liquid-blocking cap；4-5- gas-liquid separation component；4-6- gas transmission line；
4-7- cylindrical drum；4-8- back taper bottom；4-9- liquid reflux pipeline；4-10- abnormity hydraulic barrier, first piece of 4-11-
Hydraulic barrier；Second piece of hydraulic barrier of 4-12-, 4-13- third block hydraulic barrier.
Specific embodiment
The structure and application method of utility model device are further illustrated with reference to the accompanying drawing.
The exhaust system 4 of the utility model includes gas deflation assembly 4-1 and gas-liquid separation assembly 4-5, the gas deflation assembly
Including distribution grid 4-2, several liters of inflator 4-3 and with liquid-blocking cap 4-4；The gas-liquid separation component 4-5 includes gas transmission line 4-
6, the inside of cylindrical drum 4-7, back taper bottom 4-8 and liquid reflux pipeline 4-9, cylindrical drum 4-7 are provided with several
Special-shaped hydraulic barrier 4-10, every group of abnormity hydraulic barrier 4-10 are made of three pieces of hydraulic barriers, are denoted as first piece of baffling gear respectively
Plate 4-11, second piece of hydraulic barrier 4-12, third block hydraulic barrier 4-13.
The liter inflator 4-3 of the gas deflation assembly 4-1 is evenly arranged in distribution plate surface, is welded on distribution grid；Rise gas
Cylinder 4-3 shell portion is immersed in reactor liquid level hereinafter, the cylinder height being preferably submerged under liquid level is cylinder total height
1/4~1/2。
The liquid-blocking cap 4-4 of the gas deflation assembly 4-1 is connected 4-3 by gusset with liter inflator, and liquid in reactor is on the one hand made
Escaping gas from liquid-blocking cap and rises the gap outflow between inflator under face, on the other hand may be made by the limitation of the slit
Emergent gas is dissolved in feedstock oil again, reduces emergent gas amount.
It is gas-phase space, gas-phase space and external gas inside end socket on the liquid-blocking cap 4-4 of the gas deflation assembly 4-1
Liquid separation assembly is connected by gas transmission line 4-6.
One end of the gas transmission line 4-6 of the gas-liquid separation component is connected with reactor head, the other end and cylindrical shape
The lower part of cylinder 4-7 is connected.
The gas-liquid separation component 4-1 includes cylindrical drum 4-7 and back taper bottom 4-8, and cylindrical drum is located to fall
Exhaust outlet is arranged in the top of taper, the top cylindrical drum 4-7, and leakage fluid dram is arranged in back taper bottom 4-8, and leakage fluid dram is returned through liquid
Flow tube line 4-9 is connected with liquid phase connection in reactor；2N layers are arranged from the bottom to top in the cylindrical drum 4-7 of gas-liquid separation component
Baffling component, every layer of baffling component include several profiled baffle plate 4-10, wherein N >=1, and the upper limit of N is actually needed according to reaction
It determines, N preferably 2 ~ 4.Profiled baffle plate 4-10 includes that at least three pieces of hydraulic barriers 4-11,4-12,4-13 are spliced, and first piece
Hydraulic barrier 4-11 and third block hydraulic barrier 4-13 is inclined plate, and second piece of hydraulic barrier 4-12 is level board, second piece of baffling
The both ends of baffle 4-12 are separately connected first piece of hydraulic barrier 4-11 and third block hydraulic barrier 4-13, and three pieces of baffle groups are at recessed
Shape or convex structure；It is preferred that the profiled baffle plate in every layer of baffling component is identical structure；More preferably adjacent odd-level and idol
Profiled baffle plate in several layers is staggered, in further preferably adjacent odd-level and even level, the abnormity folding of odd-level
Flowing plate is concave structure, and the profiled baffle plate of even level is convex structure.Sub-dip inside the device of the liquid reflux pipeline 4-9
Not below the liquid level of reactor.
The course of work using the liquid phase hydrogenation reactor of the gas deflation assembly of the utility model is as follows：Reaction raw materials, which enter, to be added
After hydrogen reactor 1, after inlet diffuser 2 carries out rectification distribution and throttling buffering, occurs in catalyst bed 3 plus hydrogen is anti-
It answers, enters subsequent processing after reaction effluent outflow；Gas deflation assembly 4 and exhaust are provided at the top of liquid phase hydrogenation reactor 1
Mouth 5；In exhaust process, discharge gas is first via the crack risen between inflator 4-3 and liquid-blocking cap 4-4 on gas deflation assembly 4-1
Discharge, enters the gas-phase space in reactor end socket after discharge, the gas in end socket enters gas-liquid separation component 4-5, passes through first
The gas transmission line 4-6 of gas-liquid separation component 4-5 enters the lower part of cylindrical drum 4-7, wherein several groups convex or concave
The profiled baffle plate 4-10 effect of placement issues raw gas-liquid separation, and profiled baffle plate 4-10 therein is by three pieces of hydraulic barrier 4-
11,4-12,4-13 are spliced, and exhaust outlet of the gas isolated through being arranged at the top of cylindrical drum 4-7 is discharged, and isolate
Leakage fluid dram of the liquid by the setting of back taper bottom enters liquid reflux pipeline 4-9, and is soaked by the lower end liquid reflux pipeline 4-9
Do not flowed back in reactor below liquid level.
It is further illustrated below with reference to using effect of the embodiment for liquid phase hydrogenation reactor described in the utility model,
But it is not limited by following embodiments.
Comparative example 1
The virgin kerosene come from tank field is after the boosting of feedstock oil feed pump, exchanging heat to reaction temperature, with hydrogen in mixer
It is inside pre-mixed, material after mixing enters hydrogenator and liquid-phase hydrogenatin reaction, reactor head setting occurs
Conventional exhaust outlet, exhaust outlet are located at the end socket position of hydrogenator, provided with liquidometer mouth in wall of reactor, are used for
So that catalyst bed to be completely submerged under liquid level full liquid-phase hydrogenatin reaction occurs for liquid level in control and detection reactor.
Raw material oil nature is shown in Table 1；
Hydrogenation conditions and it the results are shown in Table 2.
1 feedstock property of table
Embodiment 1
The virgin kerosene come from tank field is mixed in static state with hydrogen after the boosting of feedstock oil feed pump, exchanging heat to reaction temperature
It is pre-mixed in clutch, material after mixing enters liquid phase hydrogenation reactor and liquid-phase hydrogenatin reaction, reactor occurs
Top is provided with the gas deflation assembly and exhaust outlet of the utility model, and gas deflation assembly is set to the top end socket position of hydrogenator
It sets, liquidometer mouth is provided in wall of reactor, for controlling and detecting liquid level in reactor, so that catalyst bed is complete
It is immersed under liquid level, full liquid-phase hydrogenatin reaction occurs.
The exhaust system of liquid phase hydrogenation reactor is all together the gas-liquid separation outside the gas deflation assembly and reactor in reactor end socket
Gas vent is arranged in component, reactor head, and gas vent is connect by gas transmission line with gas-liquid separation component；Gas deflation assembly packet
It includes distribution grid, several groups liter inflator and liquid-blocking cap, every group of liter inflator and liquid-blocking cap to be evenly arranged in distribution plate surface, liquid-blocking cap is logical
It crosses gusset and is connect with inflator top is risen；The distribution grid of gas deflation assembly is the sieve-plate structure of surface uniform pore openings, with hydrogenator
Inner wall is tightly connected；The liter inflator of gas deflation assembly is welded on distribution grid, rise the 1/4 of air cylinder body be immersed in reactor liquid level with
Under.4 layers of profiled baffle plate are set from the bottom to top in the drum shape cylinder body of gas-liquid separation section, and profiled baffle plate is spelled by three pieces of hydraulic barriers
It connects, first layer and third layer are convex arrangement, and the second layer and the 4th layer are arranged for spill.
Raw material oil nature is shown in Table 1；
Hydrogenation conditions and it the results are shown in Table 2.
Embodiment 2
The virgin kerosene come from tank field is mixed in static state with hydrogen after the boosting of feedstock oil feed pump, exchanging heat to reaction temperature
It is pre-mixed in clutch, material after mixing enters liquid phase hydrogenation reactor and liquid-phase hydrogenatin reaction, reactor occurs
Top is provided with the gas deflation assembly and exhaust outlet of the utility model, and gas deflation assembly is set to the top end socket position of hydrogenator
It sets, liquidometer mouth is provided in wall of reactor, for controlling and detecting liquid level in reactor, so that catalyst bed is complete
It is immersed under liquid level, full liquid-phase hydrogenatin reaction occurs.
The exhaust system of liquid phase hydrogenation reactor is all together the gas-liquid separation outside the gas deflation assembly and reactor in reactor end socket
Gas vent is arranged in component, reactor head, and gas vent is connect by gas transmission line with gas-liquid separation component；Gas deflation assembly packet
It includes distribution grid, several groups liter inflator and liquid-blocking cap, every group of liter inflator and liquid-blocking cap to be evenly arranged in distribution plate surface, liquid-blocking cap is logical
It crosses gusset and is connect with inflator top is risen；The distribution grid of gas deflation assembly is the sieve-plate structure of surface uniform pore openings, with hydrogenator
Inner wall is tightly connected；The liter inflator of gas deflation assembly is welded on distribution grid, rise the 1/2 of air cylinder body be immersed in reactor liquid level with
Under.Gas-liquid separation component can be preferred structure in the utility model, set from the bottom to top in the drum shape cylinder body of gas-liquid separation section
8 layers of profiled baffle plate are set, profiled baffle plate is spliced by three pieces of hydraulic barriers, first layer, third layer, layer 5, layer 7
For convex arrangement, the second layer, the 4th layer, layer 6 be spill arrange.
2 hydrogenation conditions of table and it the results are shown in Table 2.
Claims (10)
1. a kind of exhaust system of liquid phase hydrogenation reactor, it is characterised in that including in reactor end socket gas deflation assembly and reaction
Gas vent is arranged in gas-liquid separation component outside device, reactor head, and gas vent passes through gas transmission line and gas-liquid separation component
Connection；The gas deflation assembly includes distribution grid, several groups liter inflator and liquid-blocking cap；Every group of liter inflator and liquid-blocking cap are in distribution grid
Surface is evenly arranged, and liquid-blocking cap is connect by gusset with inflator top is risen.
2. the exhaust system of liquid phase hydrogenation reactor described in accordance with the claim 1, it is characterised in that：Point of the gas deflation assembly
Fabric swatch is the sieve-plate structure of surface uniform pore openings, is tightly connected with hydrogenator inner wall.
3. the exhaust system of liquid phase hydrogenation reactor described in accordance with the claim 1, it is characterised in that：The liter of the gas deflation assembly
Inflator is welded on distribution grid；Rise air cylinder body is partially immersed in reactor liquid level or less.
4. the exhaust system of liquid phase hydrogenation reactor described in accordance with the claim 1, it is characterised in that：The gas-liquid separation group
Part is one of gravitational settling, baffling separation, centrifuge separation, silk screen separation, filler separated structure.
5. the exhaust system of liquid phase hydrogenation reactor described in accordance with the claim 1, it is characterised in that：The gas-liquid separation group
Part is cylindrical drum and back taper bottom, and exhaust outlet is arranged at the top of gas-liquid separation component, and leakage fluid dram, row is arranged in back taper bottom
Liquid mouth is connected to through liquid reflux pipeline with liquid phase in reactor；2N layers are arranged from the bottom to top in the drum shape cylinder body of gas-liquid separation component
Baffling component, every layer of baffling component include several profiled baffle plates, wherein N >=1, and the upper limit of N is determined according to reaction actual needs.
6. the exhaust system of liquid phase hydrogenation reactor according to claim 5, it is characterised in that：Profiled baffle plate includes three
Block hydraulic barrier, first piece is inclined plate with third block, and second block of level board, second piece of both ends are separately connected first piece and third
Block, three pieces of baffle groups concavities or convex structure.
7. the exhaust system of liquid phase hydrogenation reactor according to claim 6, it is characterised in that：In every layer of baffling component
Profiled baffle plate is identical structure.
8. the exhaust system of liquid phase hydrogenation reactor according to claim 7, it is characterised in that：Adjacent odd-level and idol
Profiled baffle plate in several layers is staggered.
9. according to the exhaust system of liquid phase hydrogenation reactor described in claim 7 or 8, it is characterised in that：Adjacent odd-level
In even level, the profiled baffle plate of odd-level is concave structure, and the profiled baffle plate of even level is convex structure.
10. a kind of liquid phase hydrogenation reactor using exhaust system described in claim 1, it is characterised in that：The liquid phase
Hydrogenator further includes inlet diffuser, catalyst bed and liquid distribution trough.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820207999.0U CN208145916U (en) | 2018-02-07 | 2018-02-07 | The exhaust system of liquid phase hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820207999.0U CN208145916U (en) | 2018-02-07 | 2018-02-07 | The exhaust system of liquid phase hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208145916U true CN208145916U (en) | 2018-11-27 |
Family
ID=64382244
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820207999.0U Active CN208145916U (en) | 2018-02-07 | 2018-02-07 | The exhaust system of liquid phase hydrogenation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208145916U (en) |
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2018
- 2018-02-07 CN CN201820207999.0U patent/CN208145916U/en active Active
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