CN107474875B - A kind of method of hypergravity oil and gasoline hydrofinishing - Google Patents
A kind of method of hypergravity oil and gasoline hydrofinishing Download PDFInfo
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- CN107474875B CN107474875B CN201710865181.8A CN201710865181A CN107474875B CN 107474875 B CN107474875 B CN 107474875B CN 201710865181 A CN201710865181 A CN 201710865181A CN 107474875 B CN107474875 B CN 107474875B
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- 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
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/04—Pressure vessels, e.g. autoclaves
-
- 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
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Abstract
The invention discloses a kind of method of hypergravity oil and gasoline hydrofinishing, include the following steps: to select the concatenated first order and second level supergravity reactor；It is efficiently mixed gas-liquid two-phase is carried out in hydrogen and feedstock oil input feed cavity, is dispersed into slightly solubility hydrogen in feedstock oil and largely receives micron bubble, hydrogen reaches supersaturation in feedstock oil, forms gas-liquid mixture；Gas-liquid mixture is delivered into progress hydrogenation desulfurization and denitrogenation reaction in the rotor containing catalyst by liquid distribution trough, obtains the feedstock oil of removing sulfur-bearing nitrogen impurity；The feedstock oil input second level supergravity reactor of hydrogen and removing sulfur-bearing nitrogen impurity is subjected to hydrogenation reaction of unsaturated hydrocarbon；Reactor of the present invention can make slightly solubility hydrogen reach supersaturation in liquid phase dissolved degree, efficiently utilize reductive hydrogen, strengthen gas-liquid-solid phase mass transfer, feedstock oil desulfurization rate≤90% of this method；Denitrogenation Shuai≤80%；Compared with existing high-gravity technology, unsaturated hydrocarbons conversion ratio improves 15%.
Description
Technical field
The invention belongs to feedstock oil hydrofinishing fields, more particularly, to a kind of hypergravity oil and gasoline hydrofinishing
Method.
Background technique
It is increasingly strict with environmental regulation, low-sulfur, low aromatic hydrocarbons, high cetane number oil and gasoline have become world's hair
Up to the development trend of countries and regions oil and gasoline new spec.European Union member countries have come into effect the discharge mark of Europe V from 2009
Diesel oil sulfur content is reduced to 10 μ g/g or less by standard, the standard.The developed countries such as the U.S., Japan have also promulgated respective diesel oil mark
The standard of sulfur content is down to 15 μ g/g and 10 μ g/g or less respectively by standard.Implement state on January 1st, 2017, in the whole nation in China
The discharge standard of V.
Currently, traditional trickle bed hydrogen addition technology is mature, reliably, it is widely used in oil plant hydrogenation plant.But the work
Skill needs high score gas to recycle by circulating hydrogen compressor, and hydrogen-oil ratio is greater than 300, and high pressure line is more, and reactor is larger.Conventional
Bavin/gasoline hydrogenation is designed according to old plant, is unable to satisfy the requirement of product quality upgrading from now on.
If existing common diesel and gasoline hydrogenation technology will adapt to bavin/quality of gasoline upgrading, requirement needs are done very much
Work:
(1) conventional process techniques improvement is one trickle bed reactor of series connection after trickle bed reactor, to reduce diesel oil
Feed space velocities, to realize production the low-sulfur even needs of super-low sulfur quality.But the cost of construction can greatly increase.
(2) it is designed using existing plus hydrogen conventional processing technique, in order to produce the low-sulfur even needs of the product of super-low sulfur,
By replacing novel catalyst.But a kind of a large amount of test completion of novel catalyst needs is researched and developed, it is difficult in short cycle
Interior completion.
Therefore, it is particularly important by the improvement of engineering technology or the other hydrogen addition technology process routes of searching.It is conventional
Mainly with hydrogen mass transfer, i.e. hydrogen from gas phase diffusion and is dissolved into feedstock oil for the reactions such as desulfurization, denitrogenation in trickle bed reactor
In speed be entire hydrogenation reaction rate-determining steps.Therefore, hydrogen is dissolved in feedstock oil with the state being saturated, and eliminates hydrogen
Mass transfer influences, and subsequently enters reactor and be catalyzed with catalyst and reacts a kind of efficient hydrofinishing process of can yet be regarded as.
High-gravity technology obtains more impressive progress, CN103102942A in the application study of field of chemical engineering in recent years
Feedstock oil is successfully passed through the supergravity reactor equipped with non-precious metal catalyst, desulfurization is carried out with hydrogen counter current contacting, takes off
Nitrogen and part aromatic hydrocarbons saturated reaction, but by the way of loading catalyst, operating process is difficult, and reaction process pressure drop is larger, urges
Agent is easy inactivation；Metal-polymer catalyst is fixed on the rotor of rotating packed bed reactor by CN104419454A,
Drippolene and hydrogen pass through the catalyst bed being rotating and carry out selective hydrogenation reaction, but propose that monoblock type is urged there is no specific
The raw material proportioning and fixing means of agent fixation procedure.And in existing high-gravity technology, oil and gasoline hydrogenation reaction is because of hydrogen
It is higher to be hydrogenated into this so that hydrogenation efficiency is lower for the solubility of gas.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of methods of hypergravity oil and gasoline hydrofinishing.This method
The reactor used can make slightly solubility hydrogen reach supersaturation in liquid phase dissolved degree, efficiently utilize reductive hydrogen, strengthen gas-liquid
Solid phase mass transfer, feedstock oil desulfurization Shuai≤90% of this method；Denitrogenation Shuai≤80%；Compared with existing supergravity reactor, insatiable hunger
With hydrocarbon conversion rate Ti Gao≤15%.
Term " feedstock oil " in the present invention refers to common diesel or regular price gasoline.
In order to solve the above technical problems, invention adopts the following technical scheme that:
A kind of method of hypergravity oil and gasoline hydrofinishing, includes the following steps:
S1, selection supergravity reactor
Concatenated first order supergravity reactor and second level supergravity reactor are selected, the supergravity reactor includes
Motor, main shaft, rotor, shell and liquid distribution trough；The main shaft of the motor output end passes through housing bottom and extend into shell,
The rotor is fixed on main shaft portion；The super-gravity device further includes secondary axes, speed increaser, output shaft of the speed increaser and feed cavity；
The top of shell is arranged in the feed cavity, and the lower part of feed cavity connects liquid distribution trough；The main shaft passes through secondary axes and speedup
Device is fixedly connected, and the output shaft of the speed increaser passes through feed cavity bottom and extend into feed cavity；The output shaft of the speed increaser into
Expect that intracavitary part is equipped with stirring wing；The feed cavity is equipped with first gas inlet, liquid inlet and catalyst inlet, described
Lower part of the housing is equipped with gas liquid outlet；The upper part of the housing is equipped with gas inlet-outlet, and the housing side is equipped with second gas inlet；
S2, first order supergravity reactor motor is started, speed increaser rotation is driven, to drive the stirring wing in feed cavity
Ultrahigh speed rotation；It is efficiently mixed gas-liquid two-phase is carried out in hydrogen and feedstock oil input feed cavity, makes slightly solubility hydrogen in raw material
It is dispersed into oil and largely receives micron bubble, solubility of the hydrogen in feedstock oil reaches supersaturation, forms gas-liquid mixture；It will
Gas-liquid mixture delivers into progress hydrogenation desulfurization and denitrogenation reaction in the rotor containing catalyst by liquid distribution trough, is taken off
Except the feedstock oil of sulfur-bearing nitrogen impurity；
S3, second level supergravity reactor motor is started, speed increaser rotation is driven, to drive the stirring wing in feed cavity
Ultrahigh speed rotation；It efficiently mixes, makes by gas-liquid two-phase is carried out in the feedstock oil input feed cavity of hydrogen and removing sulfur-bearing nitrogen impurity
Slightly solubility hydrogen is dispersed into the feedstock oil of removing sulfur-bearing nitrogen impurity largely receives micron bubble, and hydrogen is molten in feedstock oil
Xie Du reaches supersaturation, forms gas-liquid mixture；Gas-liquid mixture is delivered by liquid distribution trough containing catalyst
Hydrogenation reaction of unsaturated hydrocarbon is carried out in rotor；
S4, reaction product and unreacted hydrogen pass through liquid outlet respectively and gas inlet-outlet leaves reactor.
As the further improvement of technical solution, the speed increasing ratio of the speed increaser is 1:2-500；Preferably, speed increaser
Speed increasing ratio is 1:4-25；It is highly preferred that the speed increasing ratio of speed increaser is 1:5-15.
As the further improvement of technical solution, the material of the stirring wing include titanium alloy, chromium-base alloy, dual phase steel or
Ceramics etc..
As the further improvement of technical solution, the catalyst includes structured packing catalyst or quasi- homogeneous catalyst.
Preferably, the structured packing catalyst includes basic framework, active component and Second support；The basic framework
For cordierite structured packing, the active component is combined by the testing sulphide of molybdenum or tungsten and cobalt or nickel, and Second support is
γ-Al2O3。
Preferably, the quasi- homogeneous catalyst is DNAcarrier free Ni-Mo sulfide catalyst；The quasi- homogeneous catalyst can
To be transported to feed cavity together with feedstock oil and hydrogen.
As the further improvement of technical solution, in step S2, in first order supergravity reactor, reaction pressure is
0.3-0.5MPa, temperature are 230-350 DEG C, hydrogen-oil ratio 100:1-800:1；In step S3, in second level supergravity reactor
In, reaction pressure 0.1-2MPa, temperature is 360-480 DEG C, hydrogen-oil ratio 20:1-200:1.Aforementioned condition is adapted so that with regular
The situation of filler catalyst.
As the further improvement of technical solution, in step S2, in first order supergravity reactor, reaction pressure is
0.3-0.4MPa, temperature are 200-320 DEG C, hydrogen-oil ratio 50:1-600:1；In step S3, in second level supergravity reactor
In, reaction pressure 0.1-1.5MPa；Temperature is 360-420 DEG C, hydrogen-oil ratio 20:1-100.
As the further improvement of technical solution, in step S2 and S3, the micron bubble size Control of receiving is in 30nm-
300μm。
As the further improvement of technical solution, in step S3, the control of gas-liquid-solid catalytic hydrogenation reaction residence time is
It is realized by regulation supergravity reactor revolving speed, the revolving speed of supergravity reactor can be controlled in 200-2700rpm, and liquid phase exists
The residence time can be controlled in 50-2000ms in rotor.
In the case where the one way reaction process residence time is shorter, catalytic hydroconversion rate is lower, can be by material outside
The mode of portion's circulation improves reaction conversion ratio.Revolving speed by regulating and controlling supergravity reactor is realized to molecular mixing efficiency and material
The control of residence time can reduce side reaction.
Any range documented by the present invention includes any numerical value between end value and end value and end value or end value
Between any subrange for being constituted of any number.
Unless otherwise specified, each raw material in the present invention can be obtained by commercially available purchase, equipment used in the present invention
The conventional equipment in fields can be used or carried out referring to the prior art of fields.
Compared with prior art, the invention has the following beneficial effects:
1) it is long to have the time in the liquid phase for bubble: common gas-liquid is simply mixed after bubble generates in the liquid phase in device, meeting
It rapidly rises to liquid phase surface and ruptures disappearance, it is very short there are the time；And the micro-nano generated by gas liquid high-efficiency pre-mixing apparatus
For rice bubble once generation, the rate of climb in water is slower, and the course from generating rupture generally reaches tens seconds even rather
Clock, and volume is constantly shunk in uphill process and finally dissolution disappears in water, and the smaller bubble of volume is in water
The rate of climb is slower；
2) gas-liquid mass transfer is high-efficient, and when bubble diameter is smaller, the surface tension of microbubble interface is to Bubble Characteristics
The more significant of performance is influenced, surface tension at this moment generates compression to internal gas, so that micron bubble was rising
It is constantly shunk in journey and shows itself pressurization.With the unlimited diminution of bubble diameter, the specific surface area of bubble interface is also therewith
It is unlimited to increase, finally since itself pressurized effect causes air pressure inside to increase to infinity.Therefore, it has so that more gases
It is dissolved into water across gas-liquid interface, may make that mass-transfer efficiency persistently enhances at gas-liquid interface, and micro- gas that this characteristic makes
Even if the gas content of bubble in the liquid phase reaches supersaturated condition, it may continue to the mass transport process for carrying out gas and keep efficient
Mass-transfer efficiency.Reaction and the dissolution of gas be it is simultaneous, while vapor-phase reactant is consumed, micron bubble of receiving is broken
Dissolution and macroscopical gas phase mass transfer into liquid phase are dissolved while being carried out, and gas can be supplemented within first time；
3) in terms of reducing reaction pressure: as mostly used the method for improving pressure to improve hydrogen greatly in hydrogenation plant at this stage
The dissolution of gas in the solution, such as uses gas liquid high-efficiency mixing arrangement of the invention, and liquid phase has reached before entering the reactor
Supersaturation, and since high efficient gas and liquid mixing arrangement can make Gas content in liquid phase be up to 90%, micron even nano bubble exists
The redissolution for carrying out gas phase is crushed in liquid phase, therefore the partial pressure of hydrogen can be reduced suitably in actual reactor, reduce investment at
This；
4) process is simplified, and does not need circulating hydrogen compressor, reduces investment and energy consumption, the production cost of device obviously drop
It is low；
5) supergravity reactor can greatly strengthen gas-liquid/liquid-liquid mass transfer, improve the solubility of hydrogen, and fortifying catalytic adds hydrogen
Reaction, reaction velocity is high, reactor volume is small；
6) desulfurization removing nitric significant effect can produce super-low sulfur nitrogen oil product；
7) reaction temperature rising is small, and hot localised points are not present in reactor, and catalyst is not easy coking；
8) catalyst has preferable stability and selectivity under the conditions of Continuous Liquid Phase feedstock oil hydrogen addition technology, can satisfy
The needs of industrial long-term operation；
9) monolithic catalyst active component dosage is less, does not exceed 30% generally.
In conclusion feedstock oil desulfurization Shuai≤90% of method of the invention；Denitrogenation Shuai≤80%；With existing hypergravity phase
Than unsaturated hydrocarbons conversion ratio Ti Gao≤15%.
Detailed description of the invention
Specific embodiments of the present invention will be described in further detail with reference to the accompanying drawing
Fig. 1 shows supergravity reactor structural schematic diagram of the present invention；
Fig. 2 shows the present invention to use the process flow of structured packing catalyst progress hypergravity oil and gasoline hydrofinishing
Figure；
Fig. 3 shows the process flow that the present invention carries out the hydrofinishing of hypergravity oil and gasoline using quasi- homogeneous catalyst
Figure.
Specific embodiment
In order to illustrate more clearly of the present invention, below with reference to preferred embodiment, the present invention is described further.Ability
Field technique personnel should be appreciated that following specifically described content is illustrative and be not restrictive, this should not be limited with this
The protection scope of invention.
Narration is intended merely to conveniently using the noun of locality " upper and lower, left and right " etc. in the present invention, and those skilled in the art can
Know, these orientation be it is opposite, may by rotation etc. modes change.
It is shown in Figure 1, the first supergravity reactor and second level supergravity reactor used in the present invention, including electricity
Machine 1, main shaft 2, rotor 3, shell 4 and liquid distribution trough 14；The main shaft 2 of the motor output end passes through housing bottom and extend into shell
In body 4, the rotor 3 is fixed on 2 top of main shaft；The supergravity reactor further includes that secondary axes 17, speed increaser 15, speed increaser are defeated
Shaft 6 and feed cavity 7；The top of shell 4 is arranged in the feed cavity 7, and the lower part of feed cavity 7 connects liquid distribution trough 14；Institute
State main shaft 2 and be fixedly connected with speed increaser 15 by secondary axes 17, the output shaft of the speed increaser 6 across 7 bottom of feed cavity extend into
Expect in chamber 7；The feed cavity inner part of the output shaft of the speed increaser 6 is equipped with stirring wing 11；The feed cavity 7 is equipped with the first gas
Body entrance 10, liquid inlet 8 and catalyst inlet 9,4 lower part of shell are equipped with gas liquid outlet 16；4 top of shell is equipped with
Gas inlet-outlet 12, the housing side are equipped with second gas inlet 13；Sealing 5 is equipped between rotor 3 and shell 4；
Fig. 2 show the process flow chart that structured packing catalyst carries out the hydrofinishing of hypergravity oil and gasoline.
The meaning that each section represents in figure are as follows:
18- gas bomb；19- pressure-regulating valve；20- mass flowmenter；21- gas bomb；22- pressure is adjusted
Valve；
23- mass flowmenter；24- main valve；25- check-valves；26- divides valve；27- mass flowmenter；
28- mass flowmenter；29- divides valve；30- mass flowmenter；31- ball valve；32- pump；
33- liquid supplementation pipe；34- mass flowmenter；35- ball valve；36- ball valve；37- ball valve；
38- storage tank；39- coolant；40- ball valve；41- ball valve；42- ball valve；
43- mass flowmenter；44- mass flowmenter；45- ball valve；46- divides valve；47- main valve；48- check-valves.
As shown in Fig. 2, hydrogen gas is from raw material gas cylinder 21 by needed for 22 level pressure to reaction system of pressure-regulating valve
Pressure enters first order supergravity reactor, while being passed through feedstock oil with pump 32 after then measuring by mass flowmenter 23
In level-one supergravity reactor, since stirring wing 11 and 3 high speed rotation of rotor strengthen gas-liquid mass transfer, the dissolution of hydrogen is improved
Degree makes hydrogen in feedstock oil in saturation state, and the feedstock oil of saturation reacts with the catalyst being supported on rotor 3, removes
Sulfur-bearing nitrogen impurity in feedstock oil；Then, the feedstock oil of sulfur-bearing nitrogen impurity is removed by entering two after the metering of mass flowmenter 44
Grade supergravity reactor；At the same time, the hydrogen feed gas of purification from raw material gas cylinder 18 by 19 level pressure of pressure-regulating valve to
Pressure needed for reaction system enters second level supergravity reactor after then measuring by mass flowmenter 20, carries out catalysis and adds
Hydrogen reaction；Hydrogenated products a part is sampled detection by valve 41, another by pump 36 by liquid be delivered to storage tank 38 into
Row Matter Transfer supplements fresh feed oil product by liquid supplementation pipe 33.
In certain embodiments of the present invention, the catalyst is structured packing catalyst, the structured packing catalyst
Including basic framework, active component and Second support；The basic framework is cordierite structured packing, and the active component is by molybdenum
Or the testing sulphide of tungsten and cobalt or nickel is combined into, Second support is γ-Al2O3。
In certain embodiments of the present invention, in step S2, in first order supergravity reactor, reaction pressure 0.3-
0.5MPa, temperature are 230-350 DEG C, hydrogen-oil ratio 100:1-800:1,100:1-700:1,100:1-600:1,100:1-500:
1、100:1-400:1、100:1-300:1、100:1-200:1、200:1-800:1、200:1-700:1、200:1-600:1、
200:1-500:1、200:1-400:1、200:1-300:1、300:1-800:1、300:1-700:1、300:1-600:1、300:
1-500:1,300:1-400:1,500:1-800:1,600:1-800:1 or 700:1-800:1.
In certain embodiments of the present invention, in step S3, in the supergravity reactor of the second level, reaction pressure 0.1-
2MPa, temperature are 360-480 DEG C, hydrogen-oil ratio 20:1-200:1,20:1-180:1,20:1-160:1,20:1-140:1,20:1-
120:1、20:1-100:1、20:1-80:1、20:1-60:1、20:1-40:1、50:1-200:1、50:1-180:1、50:1-
160:1、50:1-140:1、50:1-120:1、50:1-100:1、50:1-80:1、80:1-200:1、80:1-180:1、80:1-
160:1、80:1-140:1、80:1-120:1、80:1-100:1、100:1-200:1、100:1-180:1、100:1-160:1、
100:1-140:1 or 100:1-120:1.
In certain embodiments of the present invention, the speed increasing ratio of the speed increaser is 1:2-500；Preferably, the increasing of speed increaser
Speed ratio is 1:4-25；It is highly preferred that the speed increasing ratio of speed increaser is 1:5-15.
By the adjusting to speed increaser, the bubble in feed cavity 7 can be made to there is the time in the liquid phase long: common gas-liquid
It is simply mixed after bubble generates in the liquid phase in device, liquid phase surface can be rapidly risen to and rupture disappearance, it is very short there are the time；
And the micro-nano bubble generated by gas liquid high-efficiency pre-mixing apparatus, once generation, the rate of climb in water is slower, from generation
To rupture course generally reach tens seconds even a few minutes, and in uphill process volume constantly shrinks and in water finally
Dissolution disappears, and the rate of climb of the smaller bubble of volume in water is slower.
When bubble diameter is smaller, influence performance of the surface tension of microbubble interface to Bubble Characteristics is more shown
It writes, surface tension at this moment generates compression to internal gas, so that micron bubble is constantly shunk in uphill process and table
Reveal itself pressurization；With the unlimited diminution of bubble diameter, the specific surface area of bubble interface is also unlimited therewith to be increased, finally due to
Itself pressurized effect causes air pressure inside to increase to infinity；Therefore, it has so that more gases are dissolved across gas-liquid interface
Into water, may make that mass-transfer efficiency persistently enhances at gas-liquid interface, even and if this characteristic microbubble that makes in the liquid phase
When gas content reaches supersaturated condition, it may continue to carry out the mass transport process of gas and keep efficient mass-transfer efficiency.Reaction
Dissolution with gas be it is simultaneous, while vapor-phase reactant is consumed, the broken dissolution of micron bubble of receiving and macroscopical gas phase
Into liquid phase, mass transfer is dissolved while being carried out, and gas can be supplemented within first time；
It mostly uses the method for improving pressure to improve the dissolution of hydrogen in the solution in hydrogenation plant at this stage greatly, and adopts
With gas liquid high-efficiency mixing arrangement (motor 1, main shaft 2, secondary axes 17, speed increaser 15, output shaft of the speed increaser 6, stirring wing of the invention
11, feed cavity 7 etc. is collectively referred to as), liquid phase has had reached supersaturation before entering rotor, and micron even nano bubble is in liquid phase
In be crushed the redissolution for carrying out gas phase, therefore the partial pressure of hydrogen can be reduced suitably in actual reactor, reduce cost of investment.
In certain embodiments of the present invention, the material of the stirring wing includes titanium alloy, chromium-base alloy, dual phase steel or pottery
Porcelain etc..
Shown in Fig. 3, to intend the process flow chart that homogeneous catalyst carries out the hydrofinishing of hypergravity oil and gasoline.
The meaning that each section represents in figure are as follows:
49- separator；50- catalyst feeds；51- pump；52- fluid storage tanks；
53- intends homogeneous catalyst separation supplementary device；54- separator；55- catalyst feeds；56- pump；
57- fluid storage tanks；58- intends homogeneous catalyst separation supplementary device.
It is as shown in Figure 3: pressure needed for hydrogen passes through pressure-regulating valve level pressure to reaction system from raw material gas cylinder, then
Enter level-one supergravity reactor after measuring by mass flowmenter, uses pump by the desulfurization removing nitric of feedstock oil and addition at the same time
Quasi- homogeneous catalyst is passed through together in level-one supergravity reactor, since stirring wing and rotor high speed rotation are strengthened gas-liquid and passed
Matter improves the solubility of hydrogen, makes hydrogen in feedstock oil in saturation state, and the catalyst in the feedstock oil and solution of saturation occurs
Reaction removes the impurity of the sulfur-bearing nitrogen in feedstock oil；Then, reaction product is by separator 49, by primary product oil and catalysis
Agent separation, and be sent in fluid storage tanks 52；Aromatic hydrocarbons is saturated quasi- homogeneous catalytic hydrogenation catalyst and passes through catalyst feeds
50 be added in fluid storage tanks 52 mixed with product oil be sent into second level hypergravity catalytic reactor in, at the same time, hydrogen
From raw material gas cylinder by pressure needed for pressure-regulating valve level pressure to reaction system, then measured by mass flowmenter laggard
Enter second level supergravity reactor, carries out catalytic hydrogenation reaction.Reaction product is by separator 54, by secondary products oil and catalysis
Agent separation；Product a part is sampled detection by bypass, and another part enters fluid storage tanks 57；Desulfurization removing nitric is quasi- homogeneous
Catalyst is added to mix in fluid storage tanks 57 with product oil by catalyst feeds 55 is pumped into fluid storage tanks
In 59, and fresh feed oil product is supplemented by liquid supplementation pipe；Then liquid is delivered in fluid storage tanks 52 by pump and is carried out
Matter Transfer.
In certain embodiments of the present invention, the quasi- homogeneous catalyst is DNAcarrier free Ni-Mo sulfide catalyst.
In certain embodiments of the present invention, in first order supergravity reactor, reaction pressure 0.3-0.4MPa, temperature
Degree be 200-320 DEG C, hydrogen-oil ratio 50:1-600:1,50:1-550:1,50:1-500:1,50:1-450:1,50:1-400:1,
50:1-350:1、50:1-300:1、50:1-250:1、50:1-200:1、50:1-150:1、50:1-100:1、100:1-600:
1、100:1-550:1、100:1-500:1、100:1-450:1、100:1-400:1、100:1-350:1、100:1-300:1、
100:1-250:1,100:1-200:1 or 100:1-150:1；
In the supergravity reactor of the second level, reaction pressure 0.1-1.5MPa；Temperature is 360-420 DEG C, hydrogen-oil ratio 20:
1-100,20:1-80,20:1-60,20:1-40 or 20:1-20.
In certain embodiments of the present invention, the speed increasing ratio of the speed increaser is 1:2-7；Preferably, the speedup of speed increaser
Than for 1:2-5；It is highly preferred that the speed increasing ratio of speed increaser is 1:3-4.
In certain preferred embodiments of the invention, the micron bubble size Control of receiving is at 30nm-300 μm or 30nm-
250 μm or 30nm-200 μm or 30nm-150 μm or 30nm-100 μm or 30nm-50 μm or 30nm-10 μm or 30nm-1
μm or 100nm-300 μm or 100nm-250 μm or 100nm-200 μm or 100nm-100 μm or 100nm-1 μm.
In certain embodiments of the present invention, the control of catalytic hydrogenation reaction residence time is by regulation hypergravity reaction
What device revolving speed was realized, the revolving speed of supergravity reactor can be controlled in 200-2700rpm or 200-2500rpm or 200-
2000rpm or 200-1500rpm or 200-1000rpm or 200-500rpm or 400-2500rpm or 400-2000rpm,
Or 400-1500rpm or 400-1000rpm.Liquid phase residence time in rotor can be controlled in 50-2000ms.
Embodiment 1
As shown in Fig. 2, a kind of method of hypergravity straight-run diesel oil hydrofinishing, includes the following steps:
Containing derivatives such as a large amount of sulfur impurity, nitrogen in straight-run diesel oil, sulphur removal, nitrogen are gone by way of Hydrobon
Equal impurity, steps are as follows: structured packing catalyst and filler being loaded in the rotor of rotating packed bed reactor, gravity
The basic framework of monolithic catalyst in rotary drill reactor is foam γ-Al2O3.Rotating packed bed reactor is opened, is passed through
Frequency converter adjusts speed increaser (speed increasing ratio 1:3) and rotating packed bed reactor revolving speed, strengthens hydrogenation catalyst reaction；
The structured packing catalyst includes basic framework, active component and Second support；The basic framework is that violet is green
Stone structured packing, the active component are combined by the testing sulphide of molybdenum or tungsten and cobalt or nickel, and Second support is γ-
Al2O3；
Reaction condition are as follows: the pressure of level-one supergravity reactor is 0.4MPa；Temperature is 300 DEG C；Hydrogen-oil ratio is 300:1.
The pressure of second level supergravity reactor is 1.5MPa；Temperature is 400 DEG C, hydrogen-oil ratio 100:1；
Under the above-described reaction conditions, hypergravity adds gasoline parameter before and after hydrogen as shown in table 1, and the magazines derivative such as sulphur, nitrogen has
Higher removal efficiency, Cetane number improve 4 indexes；And with the increase of revolving speed, the magazines derivative removal efficiency such as sulphur, nitrogen becomes
Greatly, referring to table 2.When revolving speed is more than maximum (top) speed in table, extrusion rate variation is smaller.
Table 1: add straight-run diesel oil parameter comparison before and after hydrogen
| Oil product title | Feedstock oil 1 | Refined oil 1 | Feedstock oil 2 | Refined oil 2 |
| Density g/cm3 | 0.8248 | 0.8145 | 0.8233 | 0.8127 |
| Sulfur content m (%) | 0.711 | 0.13 | 0.860 | 0.18 |
| Nitrogen content m (%) | 0.078 | 0.008 | 0.0646 | 0.004 |
| Cetane number | 50.7 | 54.6 | 51.0 | 55.1 |
Table 2:RPB revolving speed adds the influence of hydrogen to straight-run diesel oil
It is compared with existing published supergravity reactor, such as the reactor that CN103102942A is used, material are defeated
It send and catalyst surface is directly entered by liquid distribution trough, carry out gas-liquid-solid three-phase haptoreaction, due to the alternate mixing effect of gas-liquid
Fruit is poor, and hydrogen largely escapes, and final desulfurization degree is 65% under 1600rpm operating condition；Denitrification percent is 50%；Unsaturated hydrocarbons
Conversion ratio 60%.
Embodiment 2
As shown in Fig. 2, a kind of method of hypergravity pyrolysis gasoline hydrogenation purification, includes the following steps:
Drippolene (C5—C9Component) in containing the aromatic hydrocarbons composition such as a large amount of benzene,toluene,xylene, be to obtain aromatic hydrocarbons
Valable starting materials；However the presence that will have unsaturated hydrocarbons in gasoline in gasoline, it cracks and unstable, by way of catalytic hydrogenation
So that unsaturated hydrocarbons in gasoline (monoolefine, diolefin and alkenyl arene) is become saturated hydrocarbons, while removing the impurity such as sulphur removal, nitrogen.
Reaction condition are as follows: the pressure of level-one supergravity reactor is 0.42MPa；Temperature is 320 DEG C；Hydrogen-oil ratio is 300:1；
The pressure of second level supergravity reactor is 1.8MPa；Temperature is 400 DEG C, hydrogen-oil ratio 100:1.
The structured packing catalyst includes basic framework, active component and Second support；The basic framework is that violet is green
Stone structured packing, the active component are combined by the testing sulphide of molybdenum or tungsten and cobalt or nickel, and Second support is γ-
Al2O3；
Under the above-described reaction conditions, hypergravity adds gasoline parameter before and after hydrogen as shown in table 3, and hydrogenation of unsaturated hydrocarbons is converted into full
And hydrocarbon, sulphur nitrogen have higher removal efficiency；High-gravity rotating bed revolving speed is de- to the conversion ratio of unsaturated hydrocarbons, and to impurity such as sulphur nitrogen
The affecting laws removed, the results are shown in Table 4；With the raising of RPB revolving speed, unsaturated conversion ratio increases, the removal efficiency of sulphur nitrogen increases
Greatly.When revolving speed is more than maximum (top) speed in table, extrusion rate variation is smaller.
Feed gasoline parameter comparison before and after table 3 plus hydrogen
4 RPB revolving speed of table adds the influence of hydrogen to feed gasoline
It compares with traditional supergravity reactor, such as the reactor that CN104419454A is used, is operated in 1600rpm
Under the conditions of final desulfurization degree be 70%；Denitrification percent is 60%；Unsaturated hydrocarbons conversion ratio 65%.
Embodiment 3
As shown in figure 3, a kind of method of hypergravity straight-run diesel oil hydrofinishing, includes the following steps:
Containing derivatives such as a large amount of sulfur impurity, nitrogen in straight-run diesel oil, sulphur removal, nitrogen are gone by way of Hydrobon
Equal impurity, steps are as follows:
Quasi- homogeneous catalyst is passed through revolving bed；Rotating packed bed reactor is opened, speed increaser is adjusted by frequency converter
(speed increasing ratio 1:5) and rotating packed bed reactor revolving speed strengthens hydrogenation catalyst reaction；
Reaction condition are as follows: the pressure of level-one supergravity reactor is 0.3MPa；Temperature is 280 DEG C；Hydrogen-oil ratio is 200:1.
The pressure of second level supergravity reactor is 1.2MPa；Temperature is 320 DEG C, hydrogen-oil ratio 90:1；
The quasi- homogeneous catalyst is DNAcarrier free Ni-Mo sulfide catalyst；
Under the above-described reaction conditions, hypergravity adds gasoline parameter before and after hydrogen as shown in table 5, and the magazines derivative such as sulphur, nitrogen has
Higher removal efficiency, Cetane number improve 4 indexes；And with the increase of revolving speed, the magazines derivative removal efficiency such as sulphur, nitrogen becomes
Greatly, referring to table 6.When revolving speed is more than maximum (top) speed in table, extrusion rate variation is smaller.
Straight-run diesel oil parameter comparison before and after table 5 plus hydrogen
Table 6:RPB revolving speed adds the influence of hydrogen to straight-run diesel oil
| Revolving speed/rpm | S extrusion rate (%) | N extrusion rate (%) |
| 400 | 60.8 | 70.4 |
| 800 | 87.2 | 85.8 |
| 1200 | 95.7 | 92.3 |
| 1600 | 99.5 | 99.6 |
It is compared with traditional supergravity reactor, such as the reactor that CN103102942A is used, operates item in 1600rpm
Final desulfurization degree is 58% under part；Denitrification percent is 56%；Unsaturated hydrocarbons conversion ratio 62%.
Embodiment 4
As shown in figure 3, a kind of method of hypergravity straight-run diesel oil hydrofinishing, includes the following steps:
Drippolene (C5—C9Component) in containing the aromatic hydrocarbons composition such as a large amount of benzene,toluene,xylene, be to obtain aromatic hydrocarbons
Valable starting materials.However the presence that will have unsaturated hydrocarbons in gasoline in gasoline, it cracks and unstable, by way of catalytic hydrogenation
So that unsaturated hydrocarbons in gasoline (monoolefine, diolefin and alkenyl arene) is become saturated hydrocarbons, while removing the impurity such as sulphur removal, nitrogen；It will intend
Homogeneous catalyst is passed through revolving bed；
Reaction condition are as follows: the pressure of level-one supergravity reactor is 0.22MPa；Temperature is 270 DEG C；Hydrogen-oil ratio is 180:1.
The pressure of second level supergravity reactor is 1.4MPa；Temperature is 320 DEG C, hydrogen-oil ratio 50:1；
The quasi- homogeneous catalyst is DNAcarrier free Ni-Mo sulfide catalyst；
Under the above-described reaction conditions, hypergravity adds gasoline parameter before and after hydrogen as shown in table 7, and hydrogenation of unsaturated hydrocarbons is converted into full
And hydrocarbon, sulphur nitrogen have higher removal efficiency；High-gravity rotating bed revolving speed is de- to the conversion ratio of unsaturated hydrocarbons, and to impurity such as sulphur nitrogen
The affecting laws removed, the results are shown in Table 8.With the raising of RPB revolving speed, unsaturated conversion ratio increases, the removal efficiency of sulphur nitrogen increases
Greatly.When revolving speed is more than maximum (top) speed in table, extrusion rate variation is smaller.
Table 7: add feed gasoline parameter comparison before and after hydrogen
Table 8:RPB revolving speed adds the influence of hydrogen to feed gasoline
It is compared with traditional supergravity reactor, such as the reactor that CN104419454A is used, operates item in 1600rpm
Final desulfurization degree is 72% under part；Denitrification percent is 62%；Unsaturated hydrocarbons conversion ratio 68%.
Obviously, the above embodiment of the present invention be only to clearly illustrate example of the present invention, and not be pair
The restriction of embodiments of the present invention.For those of ordinary skill in the art, may be used also on the basis of the above description
To make other variations or changes in different ways.Here all embodiments can not be exhaustive.It is all to belong to this hair
The obvious changes or variations that bright technical solution is extended out are still in the scope of protection of the present invention.
Claims (12)
1. a kind of method of hypergravity oil and gasoline hydrofinishing, which comprises the steps of:
S1, selection supergravity reactor
Select concatenated first order supergravity reactor and second level supergravity reactor；The supergravity reactor includes electricity
Machine, main shaft, rotor, shell and liquid distribution trough；The main shaft of the motor output end passes through housing bottom and extend into shell, institute
It states rotor and is fixed on main shaft portion；The super-gravity device further includes secondary axes, speed increaser, output shaft of the speed increaser and feed cavity；Institute
The top that shell is arranged in feed cavity is stated, the lower part of feed cavity connects liquid distribution trough；The main shaft passes through secondary axes and speed increaser
It is fixedly connected, the output shaft of the speed increaser passes through feed cavity bottom and extend into feed cavity；The speed increaser in feed cavity
Output shaft is equipped with stirring wing；The feed cavity is equipped with first gas inlet, liquid inlet and catalyst inlet, the shell
Lower part is equipped with gas liquid outlet；The upper part of the housing is equipped with gas inlet-outlet, and the housing side is equipped with second gas inlet；
S2, first order supergravity reactor motor is started, speed increaser rotation is driven, to drive the stirring wing superelevation in feed cavity
Speed rotation；It is efficiently mixed gas-liquid two-phase is carried out in hydrogen and feedstock oil input feed cavity, makes slightly solubility hydrogen in feedstock oil
It is dispersed into and largely receives micron bubble, solubility of the hydrogen in feedstock oil reaches supersaturation, forms gas-liquid mixture；By gas-liquid
Mixture delivers into progress hydrogenation desulfurization and denitrogenation reaction in the rotor containing catalyst by liquid distribution trough, obtains removing and contains
The feedstock oil of sulphur nitrogen impurity；
S3, second level supergravity reactor motor is started, speed increaser rotation is driven, to drive the stirring wing superelevation in feed cavity
Speed rotation；It is efficiently mixed gas-liquid two-phase is carried out in the feedstock oil input feed cavity of hydrogen and removing sulfur-bearing nitrogen impurity, makes indissoluble
Property hydrogen be dispersed into the feedstock oil of removing sulfur-bearing nitrogen impurity and largely receive micron bubble, solubility of the hydrogen in feedstock oil
Reach supersaturation, forms gas-liquid mixture；Gas-liquid mixture is delivered into the rotor containing catalyst by liquid distribution trough
Middle carry out hydrogenation reaction of unsaturated hydrocarbon；
S4, reaction product and unreacted hydrogen pass through liquid outlet respectively and gas inlet-outlet leaves reactor.
2. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: the speed increaser
Speed increasing ratio is 1:2-500.
3. the method for hypergravity oil and gasoline hydrofinishing according to claim 2, it is characterised in that: the speed increaser
Speed increasing ratio is 1:4-25.
4. the method for hypergravity oil and gasoline hydrofinishing according to claim 3, it is characterised in that: the speed increaser
Speed increasing ratio is 1:5-15.
5. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: the stirring wing
Material includes titanium alloy, chromium-base alloy, dual phase steel or ceramics.
6. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: the catalyst packet
Include structured packing catalyst or quasi- homogeneous catalyst.
7. the method for hypergravity oil and gasoline hydrofinishing according to claim 6, it is characterised in that: the structured packing
Catalyst includes basic framework, active component and Second support；The basic framework is cordierite structured packing, the active group
Divide and be combined by the testing sulphide of molybdenum or tungsten and cobalt or nickel, Second support is γ-Al2O3。
8. the method for hypergravity oil and gasoline hydrofinishing according to claim 6, it is characterised in that: described to intend homogeneously urging
Agent is DNAcarrier free Ni-Mo sulfide catalyst.
9. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: in step S2,
In first order supergravity reactor, reaction pressure 0.3-0.5MPa, temperature is 230-350 DEG C, hydrogen-oil ratio 100:1-800:
1、100:1-700:1、100:1-600:1、100:1-500:1、100:1-400:1、100:1-300:1、100:1-200:1、
200:1-800:1、200:1-700:1、200:1-600:1、200:1-500:1、200:1-400:1、200:1-300:1、300:
1-800:1、300:1-700:1、300:1-600:1、300:1-500:1、300:1-400:1、500:1-800:1、600:1-
800:1 or 700:1-800:1；
In step S3, in the supergravity reactor of the second level, reaction pressure 0.1-2MPa, temperature is 360-480 DEG C, hydrogen-oil ratio
20:1-200:1、20:1-180:1、20:1-160:1、20:1-140:1、20:1-120:1、20:1-100:1、20:1-80:1、
20:1-60:1、20:1-40:1、50:1-200:1、50:1-180:1、50:1-160:1、50:1-140:1、50:1-120:1、
50:1-100:1、50:1-80:1、80:1-200:1、80:1-180:1、80:1-160:1、80:1-140:1、80:1-120:1、
80:1-100:1,100:1-200:1,100:1-180:1,100:1-160:1,100:1-140:1 or 100:1-120:1.
10. the method for hypergravity oil and gasoline hydrofinishing according to claim 9, it is characterised in that: in step S2,
In first order supergravity reactor, reaction pressure 0.3-0.4MPa, temperature is 200-320 DEG C, hydrogen-oil ratio 50:1-600:1,
50:1-550:1、50:1-500:1、50:1-450:1、50:1-400:1、50:1-350:1、50:1-300:1、50:1-250:1、
50:1-200:1、50:1-150:1、50:1-100:1、100:1-600:1、100:1-550:1、100:1-500:1、100:1-
450:1,100:1-400:1,100:1-350:1,100:1-300:1,100:1-250:1,100:1-200:1 or 100:1-150:
1；
In step S3, in the supergravity reactor of the second level, reaction pressure 0.1-1.5MPa；Temperature is 360-420 DEG C, hydrogen oil
Than 20:1-1:5,20:1-1:4,20:1-1:3,20:1-1:2 or 20:1-1:1.
11. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: the micron of receiving
Bubble size is controlled at 30nm-300 μm or 30nm-250 μm or 30nm-200 μm or 30nm-150 μm or 30nm-100 μm,
Or 30nm-50 μm or 30nm-10 μm or 30nm-1 μm or 100nm-300 μm or 100nm-250 μm or 100nm-200 μm,
Or 100nm-100 μm or 100nm-1 μm.
12. the method for hypergravity oil and gasoline hydrofinishing according to claim 1, it is characterised in that: hypergravity reaction
The revolving speed of device is controlled in 200-2700rpm or 200-2500rpm or 200-2000rpm or 200-1500rpm or 200-
1000rpm or 200-500rpm or 400-2500rpm or 400-2000rpm or 400-1500rpm or 400-1000rpm；
Liquid phase residence time in rotor controls in 50-2000ms.
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| JP2002371286A (en) * | 2001-06-14 | 2002-12-26 | Idemitsu Kosan Co Ltd | Process for hydrogenating and purifying hydrocarbon oil |
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