CN106479562A - A kind of reinforcing dissolving method and application of the hydrogen in reformed oil - Google Patents
A kind of reinforcing dissolving method and application of the hydrogen in reformed oil Download PDFInfo
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- CN106479562A CN106479562A CN201610884864.3A CN201610884864A CN106479562A CN 106479562 A CN106479562 A CN 106479562A CN 201610884864 A CN201610884864 A CN 201610884864A CN 106479562 A CN106479562 A CN 106479562A
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- hydrogen
- oil
- reformed oil
- reinforcing
- reformed
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 125
- 239000001257 hydrogen Substances 0.000 title claims abstract description 125
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 27
- 230000003014 reinforcing effect Effects 0.000 title claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 53
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 44
- 230000003068 static effect Effects 0.000 claims abstract description 22
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 16
- 239000007791 liquid phase Substances 0.000 claims abstract description 11
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims abstract description 5
- 238000003672 processing method Methods 0.000 claims description 20
- 238000004090 dissolution Methods 0.000 claims description 19
- 239000000945 filler Substances 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 5
- 150000001336 alkenes Chemical class 0.000 abstract description 13
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 3
- 238000002407 reforming Methods 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract description 2
- 238000013386 optimize process Methods 0.000 abstract 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 28
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 17
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 17
- 229910052794 bromium Inorganic materials 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 11
- 239000002994 raw material Substances 0.000 description 10
- 238000001125 extrusion Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000011218 segmentation Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010924 continuous production 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
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- -1 olefin hydrocarbon Chemical class 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
Abstract
The present invention relates to a kind of reinforcing dissolving method of the hydrogen in reformed oil, the method is included under continuous liquid phase hydrogenation treatment conditions, first by reformed oil with hydrogen by static mixer and hydrogen-dissolving device, make hydrogen quickly mix with reformed oil reinforcing, then reforming and generating oil-off olefin reaction removing alkene is carried out in hydrogenation reactor with the catalyst with catalytic hydrogenation.The method according to the invention, on the premise of like products requirement is reached, can effectively improve reaction efficiency and production capacity, reduce the consumption of hydrogen, optimize process flow routes, it is achieved that efficient industrial production.
Description
Technical field
The invention belongs to oil product hydrofinishing field, it is more particularly related to a kind of reformed oil adds
Hydrogen fine purification treatment process.
Background technology
Reformed oil is not only rich in aromatic hydrocarbons and spirit fraction, but also containing a small amount of alkene.Therefore, reform and generate
Oil will produce suitable aromatic hydrocarbons and solvent oil product, must be freed from alkene therein.
Chinese patent CN103666544A describes a kind of recapitalization generating oil hydrogenation processing method, using at liquid-phase hydrogenatin
Under the conditions of reason, reformed oil is contacted in hydrogenation reactor with the catalyst with catalytic hydrogenation, described plus
Hydrogen used in hydrogen process is at least partially from the dissolved hydrogen in the reformed oil.The shortcoming of the technique is：Only sharp
The hydrogen dissolved with the reformed oil obtained from reformate knockout drum carries out hydrotreating, and products therefrom quality can not
Up to standard.Also need to install nano through holes additional with hydrogen make-up, equipment requirement is high.
Chinese patent CN102911721A discloses a kind of method of reformed oil liquid phase selective hydrogenation and olefin hydrocarbon removal, should
Technique is adopted under hydroconversion condition, and liquid phase mixture segmentation enters multistage conventional hydro reactor；Segmentation enters beds
Area is reacted, and is mixed from product section circulation after reactor bottom reaction out with fresh feed, partly from reaction system
Discharge follow-up separator；Internal circulating load is 1 with the ratio of raw material to described circulating liquid hydrogenation products by volume：1～
5：1；Described hydrogenation process conditions are：80～180 DEG C of reaction temperature, 1.5～2.0MPa of pressure, fresh feed volume space velocity
2.0～4.0h-1.
Chinese patent CN104560135A discloses a kind of method of hydrotreating of reformed oil, and the technique adopts reformer feed
Oil enters reforming reactor after mixing with hydrogen, and contacting with reforming catalyst carries out catalytic reforming reaction；The reforming reaction for obtaining
Effluent is directly entered recapitalization generating oil hydrogenation reactor after heat exchange, and in presence of hydrogen, being contacted with hydrogenation catalyst is carried out
Reaction；The hydrogenation reaction effluent for obtaining enters gas-liquid separator and is separated, and obtains refining reformed and generate oil and hydrogen after separating
Gas.The operating condition of recapitalization generating oil hydrogenation reactor is：Reaction pressure 1.0MPa～3.0MPa, reaction temperature 80 DEG C～200
DEG C, hydrogen to oil volume ratio 10:1～200:1,3.0～6.0h of volume space velocity-1.
In prior art, hydrogen preferably can not be dissolved in reformed oil, in order to ensure product quality, can only be kept
Less Feed space velocities, yield poorly.The hydrogen addition technology for adopting at present adopts recycle hydrogen hydrogenation technique, during being somebody's turn to do, in order to control
The reaction temperature of beds and avoid catalyst carbon deposit inactivate, generally adopt larger hydrogen-oil ratio.In catalyst during operation
The a large amount of hydrogen of bed interior circulation, it will be higher by 10 times than hydrogen amount needed for chemistry consumption hydrogen.When hydroprocessing processes adopt larger hydrogen
Oil ratio, necessarily has substantial amounts of hydrogen to have more than needed after the completion of hydrogenation reaction.These hydrogen more than needed generally all pass through hydrogen Cyclic Rings
The hydrogen charging continued after mixing after circulating hydrogen compressor supercharging as reaction is saved with new hydrogen.
When existing industry reformed oil is using hydrogen addition technology, plant construction is costly, and hydrogen circulates making an investment in for link
In whole process, the ratio of cost is very big.If the hydrogen flowing quantity in hydroprocessing processes can be reduced, can be big for enterprise
Reduce investment outlay greatly.Hydrogen how many pairs of liquid-phase hydrogenatin reactions of meltage in feedstock oil are most important, if it is possible to increase raw material
The amount of hydrogen in oil, can improve Feed space velocities, and then improve production capacity.
Content of the invention
The problem that the present invention is present for prior art, develops a kind of reinforcing hydrogen dissolution velocity in reformed oil
Processing method, the method adopt liquid-phase hydrogenatin technique, on the one hand substantially increase Feed space velocities, on the other hand reduce hydrogen
Consumption, and can operate steadily in the long term.
The invention provides a kind of processing method of reinforcing hydrogen dissolution velocity in reformed oil, the method includes：
Reformed oil and hydrogen are injected simultaneously in static mixer and are tentatively mixed, then secondary mixing is carried out in hydrogen-dissolving device,
Obtain the molten hydroforming of saturation and oil is generated, molten for saturation hydroforming is generated oil and is sent in hydrogenation reactor, at liquid-phase hydrogenatin
Under the conditions of reason, reacted with the catalyst with catalytic hydrogenation.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, described hydrogenation reaction
For prior art.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, described hydrogen-dissolving device, interior
The filler of dress corrugated metal mesh sheet.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, described hydrogen-dissolving device, interior
The location mode of the corrugated metal mesh sheet filler of dress is：Cascade type, vertical-type, the vertical mixed type of stacking.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, described static mixing
Device and hydrogen-dissolving device are connected in series, to ensure that hydrogen is quickly uniformly dissolved fully in reformed oil in continuous production.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, the molten hydrogen weight of the saturation
After whole generation oil is contacted with the catalyst with catalytic hydrogenation, separated in gas-liquid separator, gained gas phase
For hydrogen, can recycle.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, as reaction temperature is relatively low, liquid
When air speed larger so that material and catalyst contact time shorten, and olefin removal rate is high, and the degree of aromatic hydrogenation conversion substantially drops
Low, aromatic hydrocarbons is lost less than 0.3wt%.
The processing method of reinforcing hydrogen rate of dissolution in reformed oil of the present invention, wherein, described hydrogenation technique
Condition is：Reaction temperature is 120～200 DEG C；Reaction pressure is 1.0～3.0Mpa.But liquid hourly space velocity (LHSV) can bring up to：8～
18h-1；Hydrogen to oil volume ratio drops to 1～15：1
The method according to the invention, on the premise of like products requirement is reached, can effectively improve Feed space velocities, reduce hydrogen
The consumption of gas.Therefore, the recapitalization generating oil hydrogenation fine purification treatment process of the present invention optimizes process flow routes, improves product
Can, it is achieved that efficient industrial production.
Also, generated in the reformation that obtains of processing method of reformed oil rate of dissolution using the reinforcing hydrogen of the present invention
Oil, it is following that bromine index can reach 100mgBr/100g oil；Meanwhile, aromatic hydrocarbons loss amount is little, can be less than 0.5wt%.
Compared with prior art, this have the advantage that：
(1) using the hydrogen-dissolving device of the built-in corrugated metal mesh sheet filler of the present invention, it is ensured that hydrogen is in reformed oil
Interior Quick uniform dissolving, improves the Feed space velocities of reformed oil；The time reached needed for requirement conversion ratio is short, production capacity
Big purpose.
(2) hydrogen-dissolving device is used in series by the present invention with static mixer, can be rapidly achieved molten hydrogen saturation state, be made reformation
Generation oil reaches Quick uniform with hydrogen and mixes, and so as to be conducive to hydrogen quickly to dissolve in hydrogen-dissolving device, reduces disappearing for hydrogen
Consumption；
(3) the system has the characteristics that efficiency high, energy consumption be low, small volume, reduced investment, is easy to continuous prodution.Because its
Internal no-movable part, Non-energy-consumption, simple structure.
Accompanying drawing is used to be further expalined the present invention, and constitutes a part for specification, and is embodied as
Mode is used for explaining the present invention together, but is not construed as limiting the invention.
Description of the drawings
Fig. 1 is the recapitalization generating oil hydrogenation reacting flow chart for being mounted with static mixer and hydrogen-dissolving device
Wherein：1 is reformed oil, and 2 is hydrogen, and 3 is to take hydroforming to generate oil, and 4 is the molten hydroforming generation oil of saturation, 5
It is hydrofinishing reformed oil mixture, 6 is the release gas comprising undissolved hydrogen, and 7 is hydrofinishing reformed oil；A
It is static mixer, B is hydrogen-dissolving device, C is hydrogenation reactor, D is gas-liquid separator.
Specific embodiment
The invention provides a kind of processing method of reinforcing hydrogen rate of dissolution in reformed oil, the method includes：
Under liquid-phase hydrogenatin treatment conditions, by reformed oil and hydrogen successively by static mixer and hydrogen-dissolving device, then urge with having
The catalyst for changing hydrogenation is reacted in hydrogenation reactor.
According to the present invention reinforcing hydrogen rate of dissolution in reformed oil processing method, the reformed oil and
Hydrogen together enters static mixer after first mixing in the duct, turbulent flow phenomenon occurs and then is sufficiently mixed wherein, enters back into
Hydrogen is caused to be further dissolved in reformed oil in corrugated metal filler hydrogen-dissolving device.
According to the present invention reinforcing hydrogen rate of dissolution in reformed oil processing method, the reformed oil and
Hydrogen can be all continuous feed.
For ease of further illustrating the processing procedure of the present invention, the process to the present invention is described here.
As shown in figure 1, reformed oil 1 enters static mixer A with hydrogen 2 by common conduit, play is carried out wherein
Formed after strong mixing and hydroforming generation oil 3 is taken, enter back into after the molten hydroforming generation oil 4 of saturation is uniformly mixed to form in hydrogen-dissolving device B
Enter in hydrogenation reactor C, contact with the catalyst acted on hydrogenation catalyst and obtain hydrofinishing reformed oil mixture
5, enter gas-liquid separator and obtain the release gas 6 comprising undissolved hydrogen and hydrofinishing reformed oil 7.
The present invention is further explained in detail with reference to comparative example.
Comparative example 1
Using existing hydrogen addition technology (leaf bateau etc., the commercial Application [J] of HDO-18 selective hydrocatalyst. oil refine
System and chemical industry .2004,35 (8), 26～29.) catalyst is reduced and presulfurization after, hydrogen and reformed oil enter pipe
Formula hydrogenation reactor carries out recapitalization generating oil hydrogenation deolefination reaction.
Hydrogen and the hybrid mode of reformed oil：Hydrogen enters tubular type hydrogenation reaction after directly mixing with reformed oil
Device.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 10h-1, hydrogen to oil volume ratio
For 10：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.5wt%, bromine index are 385mgBr/100g oil, and alkene extrusion rate is 73.8%, aromatic hydrocarbons loss 0.5%.
Comparative example 2
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen enters pipe after mixing in static mixer with reformed oil
Formula hydrogenation reactor.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 10h-1, hydrogen to oil volume ratio
For 10：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.6wt%, bromine index are 278mgBr/100g oil, and alkene extrusion rate is 81.1%, aromatic hydrocarbons loss 0.4%.
Comparative example 3
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen mixes laggard in hydrogen-dissolving device (cascade type) with reformed oil
Enter tubular type hydrogenation reactor.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 10h-1, hydrogen to oil volume ratio
For 10：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.7wt%, bromine index are 135mgBr/100g oil, and alkene extrusion rate is 90.8%, aromatic hydrocarbons loss 0.3%.
Embodiment 1
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen with enter again to connect after the advanced static mixer of reformed oil molten
In hydrogen device (cascade type), tubular type hydrogenation reactor after mixing, is entered.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 10h-1, hydrogen to oil volume ratio
For 10：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.7wt%, bromine index are 31.6mgBr/100g oil, and alkene extrusion rate is 97.9%, aromatic hydrocarbons loss 0.3%.
Embodiment 2
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Enter string again after hydrogen and the advanced hydrogen-dissolving device of reformed oil (cascade type)
In the static mixer of connection, tubular type hydrogenation reactor after mixing, is entered.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 10h-1, hydrogen to oil volume ratio
For 10：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.7wt%, bromine index are 86.6mgBr/100g oil, and alkene extrusion rate is 94.1%, aromatic hydrocarbons loss 0.3%.
Embodiment 3
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen with enter again to connect after the advanced static mixer of reformed oil molten
In hydrogen device (vertical-type), tubular type hydrogenation reactor after mixing, is entered.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 18h-1, hydrogen to oil volume ratio
For 15：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, and product contains aromatic hydrocarbons
46.8wt%, bromine index are 92.6mgBr/100g oil, and alkene extrusion rate is 93.7%, aromatic hydrocarbons loss 0.2%.
Embodiment 4
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen with enter to connect after the advanced static mixer of reformed oil 2 again
In individual hydrogen-dissolving device (cascade type, vertical-type), tubular type hydrogenation reactor after mixing, is entered.
Reaction process condition：150 DEG C of temperature, charging reaction under pressure 1.5MPa, volume space velocity are 18h-1, hydrogen to oil volume ratio
For 4：1,1 47wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 1470mgBr/100g oil, product 46.7wt% containing aromatic hydrocarbons,
Bromine index is 54.1mgBr/100g oil, and alkene extrusion rate is 96.3%, aromatic hydrocarbons loss 0.3%.
Embodiment 5
Catalyst is reduced using existing hydrogen addition technology and presulfurization after, hydrogen and reformed oil enter tubular type and add
Hydrogen reactor carries out recapitalization generating oil hydrogenation deolefination reaction, and reaction condition is as follows：
Hydrogen and the hybrid mode of reformed oil：Hydrogen with enter again to connect after the advanced static mixer of reformed oil molten
In hydrogen device (the vertical cross-mixing type of stacking), tubular type hydrogenation reactor after mixing, is entered.
Reaction process condition：160 DEG C of temperature, charging reaction under pressure 2MPa, volume space velocity are 8h-1, hydrogen to oil volume ratio is
12：1,2 49.2wt% containing aromatic hydrocarbons of raw material (based on triphen), bromine index are 2108mgBr/100g oil, and product contains aromatic hydrocarbons
48.8wt%, bromine index are 46.2mgBr/100g oil, and alkene extrusion rate is 97.8%, aromatic hydrocarbons loss 0.4%.
The result of embodiment 1～5 shows, being used in series with respect to static mixer or molten of static mixer and hydrogen-dissolving device
The exclusive use of hydrogen device, can greatly improve Feed space velocities, and then improves yield under the same reaction conditions.
The result of embodiment 1 and 2 shows that the order that static mixer is connected with hydrogen-dissolving device is different, in same reaction conditions
Under, different impacts can be caused to reaction result, can be obtained according to the order of hydrogen-dissolving device of connecting after static mixer preferably anti-
Answer result.
Claims (6)
1. a kind of reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：Methods described includes：Will
Reformed oil and hydrogen are injected simultaneously in static mixer and are tentatively mixed, and reinjecting in hydrogen-dissolving device carries out secondary mixing,
Obtain the molten hydroforming of saturation and oil is generated, molten for saturation hydroforming is generated oil and is sent in hydrogenation reactor, manage bar at the liquid-phase hydrogenatin
Under part, haptoreaction is carried out with the catalyst with catalytic hydrogenation.
2. according to claim 1 reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：
The static mixer is connected with hydrogen-dissolving device, and static mixer and hydrogen-dissolving device are one or more.
3. according to claim 1 reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：
Add corrugated metal mesh sheet filler in the hydrogen-dissolving device.
4. according to claim 3 reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：
In the hydrogen-dissolving device, the distribution mode of filler is cascade type, vertical-type, is laminated vertical cross-mixing type.
5. according to claim 1 reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：
Liquid-phase hydrogenatin treatment conditions in the hydrogenation reactor are：The volume space velocity of reformed oil is 8～18h-1.
6. according to claim 1 reinforcing hydrogen dissolution velocity in reformed oil processing method, it is characterised in that：
Liquid-phase hydrogenatin treatment conditions in the hydrogenation reactor are：Reaction temperature is 120～180 DEG C；Reaction pressure be 1.0～
3.0Mpa；Hydrogen to oil volume ratio is 4～15：1.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109679690A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of liquid-phase hydrogenatin system and liquid phase hydrogenating method |
| CN109679682A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of molten hydrogen storage equipment and molten hydrogen methods |
| CN109679684A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of liquid-phase hydrogenatin reaction system and method |
| CN115703976A (en) * | 2021-08-04 | 2023-02-17 | 中国石油化工股份有限公司 | Method for removing olefin by liquid-phase hydrogenation of reformate |
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| CN109679690A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of liquid-phase hydrogenatin system and liquid phase hydrogenating method |
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| CN109679690B (en) * | 2017-10-19 | 2020-09-11 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation system and liquid-phase hydrogenation method |
| CN109679684B (en) * | 2017-10-19 | 2020-09-11 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reaction system and method |
| CN115703976A (en) * | 2021-08-04 | 2023-02-17 | 中国石油化工股份有限公司 | Method for removing olefin by liquid-phase hydrogenation of reformate |
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