CN106544055A - A kind of processing method of inferior heavy oil and/or poor residuum - Google Patents
A kind of processing method of inferior heavy oil and/or poor residuum Download PDFInfo
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Abstract
The present invention relates to the processing method of a kind of inferior heavy oil and/or poor residuum, the method includes to contact with hydrogenation catalyst in inferior heavy oil and/or poor residuum feeding paste state bed reactor, carry out the first hydrogenation reaction, then products therefrom is sent in high-pressure separator and is separated, hydrogen-containing gas are obtained from the top of high-pressure separator, middle part obtains liquid component and bottom obtains heavier feeds, heavier feeds are carried out into isolated deasphalted oil and the de-oiled asphalt containing hydrogenation catalyst, and the second hydrogenation reaction will be carried out in liquid component and deasphalted oil feeding fixed bed reactors, the condition of the first hydrogenation reaction causes inferior heavy oil and/or the conversion level of poor residuum to be less than 50%.The processing method of the present invention can be with the poor inferior heavy oil of handling properties and/or poor residuum, in being able to ensure that paste state bed reactor and pipeline, noncoking or coking amount substantially is less, it is possible thereby to obtain higher light oil yield, the operation cycle of fixed bed reactors is also extended.
Description
Technical field
The present invention relates to the processing method of a kind of inferior heavy oil and/or poor residuum.
Background technology
In world wide, crude oil becomes heaviness and in poor quality, resulting residual oil after crude oil time processing
Ratio is sharply increased, and the processing capacity of crude oil increases year by year in addition, and residual oil yield drastically rises.It is same with this
When, crude oil reserve is being gradually reduced, and market is increasing year by year to the demand of light-end products, light crude oil
With the price difference of heavy crude also in expanding day, it is light that residual oil/heavy oil is developed in all an urgent demands of these factors
Matter and efficient utilization new technology.
At present, residual oil/heavy oil lighting technology mainly has two processes of decarburization and hydrogenation, wherein decarburization
Journey yield of light oil is low, poor product quality, and hydrogenation process can be maximized and change into gently residual oil/heavy oil
Matter product.Hydrogen addition technology can be divided into bed technology, boiling bed technique, moving bed technique and slurry bed system
Technology, wherein bed technology are the process technologies of comparative maturity, compared to other hydrogen addition technologies, Gu
Fixed bed hydrogen addition technology is ripe, and investment cost is low, stable operation, operation safety, and good product quality is
The first-selection of hydrogen addition technology, accounts for more than the 80% of the total treating capacity of residual oil/heavy-oil hydrogenation.But, fixed bed work
There is the deficiency of two aspects in skill：One is that the adaptability to raw material is poor, when the Ni+V contents of raw material it is big
In being equal to, 200 μ g/g, micro carbon residue are more than or equal to 15 weight % or asphalt content is more than or equal to 7 weights
The difficulty processed during amount % is larger；Two is that the operation cycle is short, due to carbon deposit and metal deposit, catalyst
Inactivation is very fast.
Slurry bed technique is the technology that the checking of Jing demonstration plants can process any poor residuum/heavy oil.Slurry
Bed technique mostly using empty barrel reactor, will disperse very thin catalyst or additive and feedstock oil and
Hydrogen is converted by reactor together, in course of reaction based on heat cracking reaction, catalyst and
On the one hand the presence of hydrogen inhibits the condensation green coke of macromolecular compound, on the other hand promotes hydrogenation
Desulfurization and demetalization reaction, the catalyst for existing will also become the carrier of metal deposit, can be very big
Reactor coking is reduced in degree.Slurry bed technique main advantage includes：(1) adaptability to raw material
Extensively, the charging of any poor quality can be processed；(2) consumption of slurry bed technique additive or catalyst is few,
Product yield is high；(3) can operate at a high space velocity, the disposal ability of device can be improved；(4)
Additive or catalyst granules are little, can reduce the impact of diffusion couple reaction；(5) flow process and reactor knot
Structure is simple, it is easy to operation etc..But, the slurry bed technique developed at present is typically under high conversion
Operation, has that operating condition is harsh, product quality is poor need to carry out after-treatment, resin and asphalt
Drastic cracking cause product unstable, the easily coking in reactor and pipeline, so as to affect
The run stability of device, and the deficiency such as post catalyst reaction or additive separation difficulty, these are all
Constrain the development of slurry bed technique.
Klaus Niemann process poor residuum/heavy oil, residual oil/heavy oil and catalyst with a kind of technique
Carry out deep hydrogenation together first in slurry bed system, reaction stream is isolated into heat separator from top
Gas, isolates catalyst and portion of non-converted oil from bottom, and the logistics at middle part enters fixed bed reaction
Device carries out hydrofinishing and obtains the preferable oil product of product quality.In this process, slurry bed hydroprocessing is anti-
Condition is answered to be temperature 440-485 DEG C, pressure is 25MPa, and with this understanding, residual oil/heavy oil there occurs depth
Degree thermal cracking, is converted into light-end products, and fixed bed is simply refined to product.The method lack
Point is that serious coking is there occurs in paste state bed reactor wall and pipeline.
US 4941966 proposes the hydrotreating method of a kind of heavy oil or residual oil.The raw material of the method
It is：Heavy oil, residual oil, waste oil or its mixture, raw material are mixed with the additive of 0.1%-10.0% first
Close, additive is the solid that a class has high-specific surface area, selected from charcoal, brown mud, iron oxide, power plant
Leaching and Cyclonic dust, these additives have 2 kinds of size ranges, a kind of to be less than or equal to 90 μm, and one
Kind at 100-1000 μm, reaction condition is temperature 250-500 DEG C, pressure 5-35MPa, and hydrogen-oil ratio is
100-10000m3/t.In practical operation, this technology generally uses more than 440 DEG C of operation temperature,
The operating pressure of more than 15MPa is obtaining high conversion.The method equally there is also reactor wall and pipe
The burnt shortcoming of knot, and it is very serious.
US 5932090 proposes a kind of process inferior heavy, the method for residual oil, the method in slurry bed system
With reference to following three machining cell：Hydro-conversion is carried out using slurry bed system, product is distilled or dodged
Steam, finally carry out depitching, wherein bottoms or leave flash evaporation unit liquid have 80 weight % with
On be recycled to depitching area.In the method, slurry bed system hydrogenation unit uses oil-soluble catalyst, urges
The addition of agent is 1500-5000 μ g/g, and being hydrogenated with preferred operating condition is：Temperature 380-440 DEG C,
Pressure 10-20MPa.In this technology, the total conversion of heavy charge can reach more than 90%, resulting
Product quality also preferably, but the raising of conversion ratio rely on be bottoms or leave flash evaporation unit
The circulation of liquid, can cause reactor and pipeline coking.And this process uses oil-soluble catalysis
Agent, one side price are higher, on the other hand cannot also provide the field of enough coke and metal deposit
Institute.
US 4176051 provides the heavy oil that a kind of wherein more than 524 DEG C constituent contents of process at least account for 25%
Method, heavy oil and catalyst are made slurries at 50-400 DEG C by the method first, and are heated to
, paste state bed reactor is continuously introduced into afterwards, used reaction condition is temperature by 250-550 DEG C
400-500 DEG C, pressure 0.6-24MPa.Higher conversion ratio in the method pursuit paste state bed reactor,
Therefore the light oil yield of gained is of a relatively high, but while also produces very many cokings, more is dry
Gas, and gained light-end products need to carry out the after-treatments such as hydrofinishing, the residual oil for causing technique overall
And/or the conversion ratio of heavy oil is relatively low.
The content of the invention
It is an object of the invention to overcome the slurry of the processing method of existing inferior heavy oil and/or poor residuum
State bed reactor and pipeline coking be serious and the fixed bed reactors operation cycle short waits deficiency, there is provided one
Kind of paste state bed reactor and pipeline coking amount are less and can extend the fixed bed reactors operation cycle
The processing method of inferior heavy oil and/or poor residuum.
Although reporting more slurry bed system weight, crude conversion technology at present, these technologies typically exist
Operate under high conversion, have that operating condition is harsh, product quality is poor need to carry out after-treatment, with
And the drastic cracking of resin and asphalt causes the unstable knot easily in reactor and pipeline of product
It is burnt so as to affecting the deficiencies such as the run stability of device.
Inventor have recognized that, slurry bed system hydrogenation technique is with fixed bed hydrogenation technique in strengths and weaknesses
On define complementation, can with reference to both advantage exploitation slurry bed system-fixed bed group technology.The present invention
Inventor through further investigation find, can first by the control material in paste state bed reactor
Conversion level should not be too high, as long as and part metals therein, carbon residue and sulphur etc. can be removed, make anti-
Especially tenor and carbon residue content disclosure satisfy that fixed bed reactors feed to the residual oil property that should be generated
Requirement, then separate it is fuel-displaced in solid matter (mainly catalyst or additive) after,
Hydrogenation reaction is carried out in sending into fixed bed reactors；It is possible thereby to higher light oil yield is obtained, also
The fixed bed reactors operation cycle can be greatly prolonged, and is conducive to greatly by controlling relatively low conversion level
The big phenomenon for alleviating paste state bed reactor and pipeline coking.
The processing method that the present invention provides a kind of inferior heavy oil and/or poor residuum, the method includes will be bad
Reduced fuel oil and/or poor residuum are contacted with hydrogenation catalyst in sending into paste state bed reactor, are carried out first and are added
Hydrogen reacts, and then the first hydrogenation reaction products therefrom is sent in high-pressure separator and is separated, from height
Obtain that hydrogen-containing gas, middle part obtain liquid component and bottom obtains urging containing hydrogenation at the top of pressure separator
The heavier feeds containing hydrogenation catalyst are carried out solvent deasphalting, are taken off by the heavier feeds of agent
Coal tar and the de-oiled asphalt containing hydrogenation catalyst, and the liquid component and deasphalted oil are sent into solid
The second hydrogenation reaction is carried out in fixed bed reactor, the condition of first hydrogenation reaction causes inferior heavy oil
And/or the conversion level of poor residuum is less than 50%.
The processing method of the inferior heavy oil and/or poor residuum of the present invention exists relative to the advantage of prior art
In：
(1) applied range, can be with the poor inferior heavy oil of handling properties and/or poor residuum；
(2) in being able to ensure that paste state bed reactor and pipeline, noncoking or coking amount substantially is less, thus
Higher light oil yield can be obtained；
(3) inferior heavy oil and/or poor residuum are by carrying out the first hydrogenation first in paste state bed reactor
Reaction, disclosure satisfy that the requirement of fixed bed reactors charging, reduces fixed bed reactors hydrotreating
Difficulty, extend the operation cycle of fixed bed reactors.
Description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute the part of specification,
It is used for explaining the present invention together with detailed description below, but does not constitute the limit to the present invention
System.In the accompanying drawings：
Fig. 1 is a kind of process chart of the preferred embodiment according to the inventive method.
Fig. 2 is the process chart of another kind of preferred embodiment according to the inventive method.
Reference
1 paste state bed reactor, 2 high-pressure separator, 3 fixed bed reactors
4 solvent deasphalting towers
Specific embodiment
Hereinafter the specific embodiment of the present invention is described in detail.It should be appreciated that this place
The specific embodiment of description is merely to illustrate and explains the present invention, is not limited to the present invention.
The invention provides the processing method of a kind of inferior heavy oil and/or poor residuum, the method include by
Inferior heavy oil and/or poor residuum are contacted with hydrogenation catalyst in sending into paste state bed reactor, carry out first
Hydrogenation reaction, then sends into the first hydrogenation reaction products therefrom in high-pressure separator and is separated, from
Obtain at the top of high-pressure separator that hydrogen-containing gas, middle part obtain liquid component and bottom is obtained containing hydrogenation
The heavier feeds containing hydrogenation catalyst are carried out solvent deasphalting, are obtained by the heavier feeds of catalyst
Deasphalted oil and the de-oiled asphalt containing hydrogenation catalyst, and the liquid component and deasphalted oil are sent into
The second hydrogenation reaction is carried out in fixed bed reactors, the condition of first hydrogenation reaction causes inferior heavy
The conversion level of oil and/or poor residuum is less than 50%.
In the present invention, term " conversion level " refers to (inferior into the feedstock oil of paste state bed reactor
Heavy oil and/or poor residuum) conversion ratio, the method for testing of conversion ratio is according to ASTM D7169-11
The High Temperature Simulation way of distillation that standard is carried out.
In the present invention, when all inferior heavy oils into paste state bed reactor, the amount of feedstock oil refers to
Into the amount of the inferior heavy oil of paste state bed reactor；When all poor residuums into paste state bed reactor
When, the amount fingering of feedstock oil enters the amount of the poor residuum of paste state bed reactor；When entering paste state bed reactor
Existing inferior heavy oil when having poor residuum again, the amount fingering of feedstock oil enters the inferior heavy of paste state bed reactor
The total amount of oil and poor residuum.
In the present invention, the original that " heavy oil " refers to asphalitine and gum level is higher, viscosity is larger
Oil, its ground surface density are more than 0.943g/cm3And underground viscosity is more than 50 centipoises." residual oil " is referred to
The remaining component in destilling tower bottom during crude distillation.Wherein, the crude oil is referred to from underground mining out
Natural oil, it is a kind of liquid, the mineral products with hydrocarbon as main component.
In the present invention, inferior heavy oil and poor residuum continue to use the conventional definition in this area, refer to quality
Poor heavy oil and residual oil, refer in particular to those tenors and/or carbon residue the higher heavy oil of content and
Residual oil.Preferably, in the poor residuum and/or inferior heavy oil, tenor is at least 110 μ g/g, residual
Carbon content is at least 10wt%；It is highly preferred that tenor in the poor residuum and/or inferior heavy oil
At least 180 μ g/g, carbon residue content are at least 15wt%.
It was found by the inventors of the present invention that in the first hydrogenation reaction, if conversion level is too high, easily
Reactor and pipeline coking are caused, so as to affect the stability of plant running, therefore, in the first hydrogenation
In reaction, should control in paste state bed reactor is guaranteed on the premise of noncoking, will be second-rate
The most of metal of raw material removing and transform portion carbon residue the removing with part sulphur etc., generate reaction
Heavy oil or residual oil property especially tenor and carbon residue content disclosure satisfy that fixed bed reactors feed
Requirement.The present inventor further study show that, by controlling the first hydrogenation reaction
Condition causes inferior heavy oil and/or the conversion level of poor residuum that above-mentioned mesh is capable of achieving less than 50%
's.And the prior art yield of light oil higher in order to pursue paste state bed reactor, inferior heavy oil and/or
The conversion level of poor residuum typically up to more than 80%, as a result causes a large amount of cokings, not only light oil
Product yield is not improved, and is also resulted in subsequent catalyst and is easily inactivated.The present inventor is in process of the test
Middle discovery, when the conversion level of inferior heavy oil and/or poor residuum in the first hydrogenation reaction is less than 50%
When, in inferior heavy oil and/or poor residuum, tenor can be typically removed to below 80 μ g/g, carbon residue
Content can typically be reduced to 15%, and be able to ensure that toluene insolubles (that is, green coke amount) 1.6%
Below；Preferably, in the first hydrogenation reaction, the conversion level of inferior heavy oil and/or poor residuum is
20-50%, more preferably 25-50%, thus further improve light in the case where metal removal rate is ensured
Matter oil yield.
In the present invention, method of the tenor (weight %) according to ASTM D5708 in liquid material
Determine, carbon residue content (weight %) is determined according to the method for ASTM D4530, sulfur content (weight %)
According to ASTM D5291-96 method determine, toluene insolubles content (weight %) according to
The method of GB8926TOL is determined.
In a kind of specific embodiment of the present invention, the product obtained by the first hydrogenation reaction enters high pressure
It is allowed to stand in separator and natural separation occurs, containing for nature rising is obtained from the top of high-pressure separator
Hydrogen, bottom obtain the heavier feeds of the muddy containing hydrogenation catalyst of natural subsidence, and middle part is flowed
The liquid component of state, the liquid component of the fluidised form carry out second in being sent directly into fixed bed reactors
Hydrogenation reaction.The heavier feeds that bottom obtains can be controlled by controlling the time for standing to obtain with middle part
Liquid component ratio.In order to obtain liquid product yield as high as possible, the general time for standing makes
Obtain 10 weight % of the amount less than paste state bed reactor inlet amount of bottom heavier feeds.
It was found by the inventors of the present invention that by the weight containing hydrogenation catalyst for obtaining high-pressure separator bottom
What matter material was passed through that solvent deasphalting tower is separated into lighter deasphalted oil and heavy contains hydrogenation catalyst
De-oiled asphalt, and by deasphalted oil feeding fixed bed reactors carry out the second hydrogenation reaction, just can be big
The big time for shortening even completely left out high-pressure separator standing is (general by controlling going out for high-pressure separator
Material speed is controlling), and without the need for the filter in traditional handicraft or other be used to remove in liquid component
The equipment of catalyst.By increasing solvent deasphalting step, the time that can control to stand causes bottom weight
30 weight % of the amount of matter material less than paste state bed reactor inlet amount, general control is in 15-30 weights
Amount %, more preferably 25-30 weight %, it is possible thereby to obtain solvent deasphalting load and yield it
Between preferable economic equilibrium.And prior art is in order to obtain higher liquid component yield, it usually needs control
The amount of bottoms material processed is less than 20 weight %, and general control is in 10-15 weight %.Thus, using this
The method of invention, the process load of high-pressure separator can reduce half.Also, can also contain and add
The de-oiled asphalt of the heavy of hydrogen catalyst is at least partly back to paste state bed reactor, on the one hand can drop
Low cost, reduction waste discharge, on the other hand, due to wherein containing substantial amounts of useless/old catalyst, more
Be conducive to control conversion level relatively low so as in the range of application claims.Wherein, it is back to slurry bed system
There is no particular limitation for the amount of the de-oiled asphalt containing hydrogenation catalyst of reactor, it is preferable that accounts for
Paste state bed reactor feeds 0.5-20 weight % of total amount, more preferably accounts for 1-15 weight %, further preferably
For 1-5 weight %.
In the present invention, there is no particular limitation for the species of the solvent that the solvent deasphalting is used, and uses
The conventional solvent deasphalting in this area carries out the detached solvent of mink cell focus with solvent, for example, can be third
One or more in alkane, butane, pentane and hexane.Solvent deasphalting is typically in solvent deasphalting tower
Carry out.In the solvent deasphalting tower, there is no particular limitation for the consumption of solvent, it is preferable that relative to 100
The heavier feeds of the entrance solvent deasphalting tower of weight portion, the consumption of solvent is 10-25 weight portions, preferably
For 10-16 weight portions.Also there is no particular limitation for the operating condition of solvent deasphalting tower, can be according to this
The conventional operating condition in field is carried out, it is preferable that pressure is 2.8-3.9MPa, and tower top temperature is 54-82 DEG C,
Preferably 70-82 DEG C.
According to a kind of specific embodiment of the invention, as shown in figure 1, reaction mass and catalyst are (preferably
With up flow type from bottom to top) contact that to carry out the first hydrogenation anti-in paste state bed reactor 1 with hydrogen
Should, reaction resulting material is separated into high-pressure separator 2, is obtained from the top of high-pressure separator 2
Naturally (content is generally less than 1 weight % to the hydrogen-containing gas for rising, usually 0.4-0.7 weight %, to starch
State bed reactor feeds gauge), middle part obtains the lighter liquid component for being practically free of hydrogenation catalyst and (contains
Amount is generally 70-75 weight %, feeds gauge with paste state bed reactor), bottom is obtained containing hydrogenation catalyst
Heavier feeds (as above, content is usually no more than 30 weight %, usually 25-30 weight %, with starch
State bed reactor feeds gauge), the heavier feeds containing hydrogenation catalyst that bottom obtains are sent into into solvent
Further isolated lighter deasphalted oil and heavy are carried out in deasphalting tower 4 contains hydrogenation catalyst
De-oiled asphalt, deasphalted oil is merged or is each sent with the liquid component without hydrogenation catalyst at middle part
The second hydrogenation reaction is carried out in entering fixed bed reactors 3, by the de-oiled asphalt part containing hydrogenation catalyst
Or recycle in being all returned to paste state bed reactor 1, or directly outer row.
For the phenomenon of coking in further reducing paste state bed reactor and pipeline, the present inventor is also
It was found that, if fixed bed reactors outlet resulting material is at least partly back to paste state bed reactor, can
It is not produce coking in guaranteeing substantially paste state bed reactor and pipeline, more inferior so as to be more beneficial for processing
Heavy oil and/or residual oil and extend operation cycle of fixed bed, its principle may is that：Fixed bed reaction
The light material of device outlet gained on the one hand can be effectively prevented in paste state bed reactor poor residuum and/
Or the asphalitine in heavy oil is separated out or the asphalitine of precipitation is dissolved again, on the other hand can also be played
The effect of hydrogen supply agent.Can preferably suppress the feelings of coking phenomenon by controlling conversion level in the present invention
Under condition, the process of the return material is used merely as further optimizing the invention effect of the present invention, because
There is no particular limitation for the amount of this return material；The preferable invention effect of collateral security (coking amount is low, plus
Work inferior heavy oil and/or residual oil, extend operation cycle of fixed bed etc.) and the enough yield of guarantee consideration
Set out, it is preferable that the fixed bed reactors for being back to paste state bed reactor export the amount of resulting material
1-20 weight % that paste state bed reactor feeds total amount, more preferably 1-15 weight % are accounted for, it is further excellent
Elect 5-10 weight % as.
According to a kind of preferred embodiment of the invention, as shown in Fig. 2 which is included in Fig. 1
On the basis of shown specific embodiment, fixed bed reactors 3 are exported into resulting material part and is back to
Paste state bed reactor 1, remainder become product or enter subsequent handling.
The processing method of the present invention can also include carrying out the liquid component of gained in the middle part of high-pressure separator
Further separate to be re-fed into carrying out after removing contained hydrogenation catalyst described the in fixed bed reactors
Two hydrogenation reactions；Wherein, the mode for being separated off contained hydrogenation catalyst in the liquid component
The liquid component can be sent into filter and/or switchable guard bed reactor.The present invention's adds
Work method can also include heavier feeds or the solvent deasphalting tower bottom for obtaining 2 bottom of high-pressure separator
The de-oiled asphalt, and/or the liquid component for obtaining is sent into through the material containing catalyst that filter is obtained
Vacuum fractionation is carried out in vacuum fractionation tower, and the light component for obtaining is sent into together with the liquid component
The second hydrogenation reaction is carried out in fixed bed reactors；The light component that vacuum fractionation is obtained is referred to when using decompression
Fractionating column carries out overhead fraction during vacuum fractionation.The present invention is provided with solvent deasphalting tower, actually
Jing is provided with the function of filter, switchable guard bed reactor and vacuum fractionation tower, therefore from simplifying
Flow process, cost-effective angle are set out, and the present invention preferably no longer arranges the use in addition to solvent deasphalting tower
In filtering catalyst or the equipment of separation component.
In the present invention, there is no particular limitation for the operating condition of the high-pressure separator, can basis
The requirement of resulting material is suitably adjusted, such as the operating condition of described high-pressure separator can be wrapped
Include：Temperature is 350-420 DEG C, and pressure is 6-16MPa；Preferably, the operation of the high-pressure separator
Condition includes：Temperature is 360-400 DEG C, and pressure is 8-12MPa.The equipment choosing of the high-pressure separator
With the conventional equipment in this area.
In the present invention, it is preferred to, all materials for being back to paste state bed reactor account for paste state bed reactor
1-20 weight % of charging total amount, more preferably 1-15 weight %；It is described " all to be back to slurry bed system
The material of reactor " includes the de-oiled asphalt for being back to paste state bed reactor, the possible fixation
Bed reactor outlet resulting material, and the total amount of the material of the needs return of presumable other equipment.
In the present invention, paste state bed reactor charging total amount refers to fresh inferior heavy oil and/or residual oil and above-mentioned
The total amount of all materials for being back to paste state bed reactor.
In the present invention, there is no particular limitation for the operating condition of the paste state bed reactor, Neng Gouman
Requirement of the foot to conversion level.It was found by the inventors of the present invention that when temperature is higher than 430 DEG C, slurry
The temperature in obvious coking phenomenon, therefore present invention control paste state bed reactor occurs in state bed reactor
Degree is less than 430 DEG C, preferably more than 420 DEG C.Specifically, the operation bar of the paste state bed reactor
Part can include：Temperature is 330-420 DEG C, and hydrogen dividing potential drop is 6-25MPa, and hydrogen to oil volume ratio is
100-10000, air speed are 0.1-0.5h-1；Preferably, the operating condition bag of the paste state bed reactor
Include：Temperature is 350-420 DEG C, and hydrogen dividing potential drop is 10-20MPa, and hydrogen to oil volume ratio is 200-5000, air speed
For 0.1-0.3h-1.Unless otherwise stated, air speed of the present invention refers to liquid hourly space velocity (LHSV).Relate in the present invention
And volume refer both to the volume under standard state (273K, 0.1MPa).
According to the present invention, in the first hydrogenation reaction, with the fresh feed oil into paste state bed reactor
Weight on the basis of, the addition of the hydrogenation catalyst can be 1-10 weight %.In the present invention,
" fresh " feedstock oil is for the aftermentioned material for returning paste state bed reactor, i.e., to enter for the first time
The feedstock oil of paste state bed reactor.Theoretically, the addition of catalyst of the invention is more big more favourable
In the carrying out of reaction, but, if catalyst is excessive, reaction system solid content can be caused too high, from
And the abrasion of acceleration pump, and catalyst consumption it is excessive be also easily caused conversion level control difficulty add
Greatly, therefore, consider the control of catalytic performance, service life of equipment and conversion level, the hydrogenation urges
The addition of agent is preferably 2-8 weight %.
According to the present invention, in the first hydrogenation reaction, the hydrogenation catalyst can be at various hydrogenation
Reason catalyst and its mixture, for example, can be fresh catalyst and/or useless/old hydrotreating catalyst.
It was found by the inventors of the present invention that by using various existing useless/old hydrotreating catalysts, not only may be used
With reduces cost, and conversion level can also be better controled in the range of application claims, thus
Useless hydrotreating catalyst also for prior art have found new outlet.In the present invention, at the hydrogenation that gives up
Even if reason catalyst referring to that carried out after being recycled for a long time that again regeneration is processed can not reach at hydrogenation
The discarded hydrotreating catalyst of reason Active pharmaceutical.Old hydrogenation catalyst is referred to used but is passed through
The hydrotreating catalyst for using is may continue to after regeneration.As useless/old hydrotreating catalyst is relative to new
Fresh dose the features such as there is carbon deposit and/or inactive metal such as content of vanadium is high, thus the present invention with carbon content with/
Or content of vanadium is representing whether catalyst is useless/old catalyst.Usually, fresh dose of carbon content and vanadium contain
Amount essentially 0, and the carbon content of useless hydrotreating catalyst can be up to 20 weight %, content of vanadium is more
It is up to 30 weight %.The de-oiled asphalt containing hydrogenation catalyst is at least partly returned by the present invention
The first hydrogenation reaction is participated in into paste state bed reactor, equivalent to adding in warp-wise paste state bed reactor
Useless/old hydrotreating catalyst, in this case, adds the hydrorefining catalyst in paste state bed reactor
Agent can also can be useless/old hydrotreating catalyst, preferably fresh catalyst for fresh catalyst.
When using useless/old catalyst, on the basis of the total amount of catalyst, the carbon of the hydrogenation catalyst
Content is preferably 1-20 weight %, more preferably 5-15 weight %, the content of vanadium of the hydrogenation catalyst
With V2O5Meter is preferably 1-30 weight %.The content of wherein carbon is pressed the method for GB/T17144-1997 and is surveyed
Fixed, tenor such as content of vanadium is determined by inductively coupled plasma emission spectrography.
When using useless/old catalyst, present inventor have further discovered that, the use of granularity is 100-400 mesh
Useless/old hydrotreating catalyst, can further improve the yield of light oil.Can be by using it
Before be ground so that uniform particle sizes meeting above-mentioned preferred Particle size requirements.The method and apparatus of grinding
The method and apparatus that this area can be adopted conventional, the useless hydrotreating catalyst after grinding can be by sieves
Point-score selects particle diameter to be not less than 100 mesh, for example, 100-400 mesh, and preferably 100-200 purposes are useless adds
Hydrogen processes catalyst.
According to the present invention, in the first hydrogenation reaction, the hydrogenation catalyst includes carrier and is supported on
Active metal component on the carrier, the active metal component are selected from vib metals and/or the
One kind or many in one or more in VIII base metal, preferably molybdenum, tungsten, nickel and cobalt
Kind.The content of active metal component is usually the 7-45% of total catalyst weight and is preferably 7-35%, VIB
5-20% of the content of race's metallic element for total catalyst weight.The carrier can be aoxidized for porous, inorganic
One or more in thing, such as aluminum oxide, silica and amorphous silica-alumina, more preferably aluminum oxide.
Can for example be Research Institute of Petro-Chemical Engineering suitable for the hydrogenation catalyst of paste state bed reactor of the present invention
RCS and/or RMS series hydrogenation catalyst.
In the present invention is a kind of preferred embodiment, for the hydrogenation catalyst of paste state bed reactor, with
On the basis of the weight of the hydrogenation catalyst, wherein the content of each composition is：γ-Al2O3For 55-90 weights
Amount %, Co2O3For 0-5 weight %, MoO3For 5-20 weight %, NiO is 0-3 weight %, V2O5
For 0-30 weight %, and C is 5-15 weight %；Additionally, it is possible to also contain a small amount of SiO2With/
Or P2O5And other inevitable impurity.
According to the present invention, in the first hydrogenation reaction, the hydrogenation catalyst can be with this area routine
State addition, preferably powder, and particle diameter is selected not less than 100 mesh by sieve method, for example,
100-400 mesh, the preferably hydrogenation catalyst of 100-200 mesh.
In the present invention, second hydrogenation reaction is carried out in fixed bed reactors, by above
Process, especially tenor and carbon residue content disclosure satisfy that fixed bed reactors to the property of resulting material
The requirement of charging, reduces the difficulty of fixed bed reactors hydrotreating, in fixed bed reactors,
The removal efficiency of the impurity of material can reach more than 98%.The operating condition of the fixed bed reactors can
To include：Pressure is 7-22MPa, and reaction temperature is 350-450 DEG C, and air speed is 0.1-0.5h-1, hydrogen oil
Volume ratio is 350-2000；Preferably, the operating condition of the fixed bed reactors includes：Pressure is
8-20MPa, reaction temperature are 350-420 DEG C, and air speed is 0.1-0.3h-1, hydrogen to oil volume ratio is
800-1200。
According to the present invention, in the second hydrogenation reaction, the hydrogenation catalyst loaded in fixed bed reactors
Agent can it is identical from the hydrogenation catalyst used by paste state bed reactor can also be different.For example, fixed bed
The hydrogenation catalyst loaded in reactor includes carrier and load active metal group on this carrier
Point, the one kind of the active metal component in vib metals and/or group VIII base metal
Or various, one or more preferably in molybdenum, tungsten, nickel and cobalt, it is further preferred that fixed bed
The combination of the active metal component of the hydrogenation catalyst loaded in reactor be nickel-tungsten, nickel-tungsten-
Cobalt, nickel-molybdenum or cobalt-molybdenum.The content of active metal component can be the 9-27% of total catalyst weight,
6-20% of the content of group vib metallic element for total catalyst weight.The carrier can be porous, inorganic
One or more in oxide, such as aluminum oxide, silica and amorphous silica-alumina, more preferably aoxidize
Aluminium.Can for example be the catalysis of sinopec Chang Ling suitable for the hydrogenation catalyst of fixed bed reactors of the present invention
The residual oil hydrocatalyst of the RCS and/or RMS series of agent company.
According to the present invention, the property of the light oil obtained by after the second hydrogenation reaction can reach S contents and be
Below 0.6 weight %, Ni+V contents are below 35 weight %, and carbon residue content is below 10 weight %,
The content of toluene insolubles is below 2 weight %；Preferably, after the second hydrogenation reaction gained light oil
Property can reach S contents for below 0.4 weight %, Ni+V contents are below 20 weight %, residual
Carbon content is below 6 weight %, and the content of toluene insolubles is below 1.6 weight %.Also, generally
In the case of, after the second hydrogenation reaction of the invention, the product yield of the clean or white of gained can reach 80%
More than, preferably reach more than 85%.
In the present invention, the computational methods of product yield are that liquid obtained by unit time fixed bed reactors is produced
Quality/unit interval enters the raw material oil quality of paste state bed reactor.
Below, more detailed description is done to the present invention by embodiment.
The assay method of each parameter is in the following Examples and Comparative Examples：
Density (20 DEG C)/(gcm-3) determine according to the method for GB/T 2540；
Viscosity (100 DEG C)/(mm2·s-1) determine according to the method for ASTM D445；
Carbon residue content (weight %) is determined according to the method for ASTM D4530；
Asphalt content (weight %) is determined according to the method for SH/T 0509-2010；
S contents (weight %) are determined according to the method for ASTM D5291-96；
N content (weight %) is determined according to the method for ASTM D5291-96；
Tenor (μ g/g) is determined according to the method for ASTM D5708；
The content (weight %) of toluene insolubles is determined according to the method for GB8926TOL, toluene insoluble
The content of thing can represent green coke amount, and the content of toluene insolubles is higher, and green coke amount is higher, and slurry bed system is anti-
Answer device and the easier coking of pipeline.
In the following Examples and Comparative Examples, capacity of returns refers to the unit interval and returns to paste state bed reactor
Material amount account for unit interval paste state bed reactor feed total amount percentage by weight；
Product yield=(liquid product mass obtained by unit interval fixed bed reactors-unit interval fixed bed
Reactor outlet resulting material is back to the liquid product mass of paste state bed reactor)/unit interval entrance slurry
The raw material oil quality of state bed reactor；Slurry bed system is back to when fixed bed reactors not being exported resulting material
During reactor, described " unit interval fixed bed reactors outlet resulting material is back to paste state bed reactor
Liquid product mass " for 0.Wherein, raw material oil quality refers to the quality of fresh feed oil, works as presence
When the above return is operated, the back amount from materials such as high-pressure separator bottoms is not included.
The property of feedstock oil A and B used by following examples and comparative example is as shown in table 1, used
The property of catalyst C, D, E, F and G is as shown in table 2.
Table 1
Table 2
Note：In upper table, "-" is represented and be can't detect
Embodiment 1
With A as raw material (property is shown in Table 1), in paste state bed reactor, with C as catalyst, (property is shown in Table
2), material flow figure is as shown in Figure 1.
It is 100-150 mesh to grind and control particle diameter by sieve method catalyst, with fresh feed weight of oil
3.0 weight % add in paste state bed reactor 1 with raw material and hydrogen from bottom to top.Control slurry
Bed reactor 1 operating condition be：420 DEG C of temperature, pressure 10MPa, hydrogen to oil volume ratio 1000 are empty
Fast 0.2h-1.The conversion level of 1 outlet material of paste state bed reactor is as shown in table 3.Material is from slurry bed system
High-pressure separator 2 is entered in reactor 1, the operating condition of high-pressure separator 2 includes 380 DEG C of temperature,
Pressure 10MPa, and control the discharging speed of high-pressure separator so that 2 bottom of high-pressure separator obtains
Heavier feeds account for 25 weight % of paste state bed reactor inlet amount, obtain from the middle part of high-pressure separator 2
The amount of liquid component accounts for 74 weight % of paste state bed reactor inlet amount.
By isolated deasphalted oil in above-mentioned heavier feeds feeding solvent deasphalting tower 4 and containing hydrogenation catalyst
The de-oiled asphalt of agent, the operating condition of solvent deasphalting include solvent for propane, propane and heavier feeds
Weight ratio is 1：8, tower top temperature is 80 DEG C, and pressure is 3.0MPa, and deasphalted oil is separated with high pressure
The liquid component obtained in the middle part of device 2 is sent in fixed bed reactors 3 together, will be de- containing hydrogenation catalyst
An oil asphalt part is back to paste state bed reactor 1, arranges outside remainder, and capacity of returns is 3.0 weights
Amount %.
The operating condition of fixed bed reactors 3 includes：Pressure is 15MPa, and reaction temperature is 400 DEG C,
Air speed is 0.2h-1, hydrogen to oil volume ratio is 1000；The catalyst loaded in fixed bed reactors 3 is Chang Ling
The hydrogenation catalyst of the RCS trades mark of catalyst Co. production.Product yield is as shown in table 3.
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported is shown in Table 3.
Embodiment 2
With B as raw material (property is shown in Table 1), in paste state bed reactor, with D as catalyst, (property is shown in Table
2), material flow figure is as shown in Figure 1.
It is 120-180 mesh to grind and control particle diameter by sieve method catalyst, with fresh feed weight of oil
5.0 weight % add in paste state bed reactor 1 with raw material and hydrogen from bottom to top.Control slurry
Bed reactor 1 operating condition be：380 DEG C of temperature, pressure 12MPa, hydrogen to oil volume ratio 1500 are empty
Fast 0.1h-1.The conversion level of 1 outlet material of paste state bed reactor is as shown in table 3.Material is from slurry bed system
High-pressure separator 2 is entered in reactor 1, the operating condition of high-pressure separator 2 includes 390 DEG C of temperature,
Pressure 9MPa, and control the discharging speed of high-pressure separator so that 2 bottom of high-pressure separator obtains
Heavier feeds account for 30 weight % of paste state bed reactor inlet amount, obtain from the middle part of high-pressure separator 2
The amount of liquid component accounts for 69.5 weight % of paste state bed reactor inlet amount.
By above-mentioned heavier feeds are into isolated deasphalted oil in solvent deasphalting tower 4 and contain hydrogenation catalyst
The de-oiled asphalt of agent, the operating condition of solvent deasphalting include solvent for butane, butane and heavier feeds
Weight ratio is 1：10, tower top temperature is 75 DEG C, and pressure is 3.5MPa, by deasphalted oil and high pressure point
The liquid component obtained in the middle part of device 2 is sent in fixed bed reactors 3 together, will contain hydrogenation catalyst
A de-oiled asphalt part is back to paste state bed reactor 1, arranges outside remainder, and capacity of returns is 4.0 weights
Amount %.
The operating condition of fixed bed reactors 3 includes：Pressure is 12MPa, and reaction temperature is 380 DEG C,
Air speed is 0.2h-1, hydrogen to oil volume ratio is 800；The catalyst loaded in fixed bed reactors 3 is urged for Chang Ling
The hydrogenation catalyst of the RDM trades mark of agent company production.Product yield is as shown in table 3.
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported is shown in Table 3.
Comparative example 1
Method according to embodiment 2 is carried out, except that, the control operation bar in paste state bed reactor
Part be 460 DEG C of temperature, pressure 15MPa, hydrogen to oil volume ratio 2000, air speed 0.1h-1。
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported, conversion are deep
Degree and product yield are shown in Table 3.As can be seen from Table 3, the toluene insoluble of the outlet of paste state bed reactor 1
The content of thing is apparently higher than embodiment 1 and embodiment 2.
Comparative example 2
Method according to embodiment 2 is carried out, except that, make the material from paste state bed reactor 1
Sufficient standing separation is carried out in high-pressure separator 2 so that the heavy thing that 2 bottom of high-pressure separator obtains
Material accounts for 15 weight % of paste state bed reactor inlet amount, the liquid group obtained from the middle part of high-pressure separator 2
The amount divided accounts for 85 weight % of paste state bed reactor inlet amount, and 2 bottom of high-pressure separator is obtained
Heavier feeds do not enter in solvent deasphalting tower 4 and separate, but directly outer arrange；In high-pressure separator 2
The liquid component that portion obtains first passes through filter and filters out the hydrogenation catalyst wherein carried secretly, is then fed into solid
In fixed bed reactor 3.
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported, conversion are deep
Degree and product yield are shown in Table 3.As can be seen from Table 3, the toluene insoluble of the outlet of paste state bed reactor 1
The content of thing is apparently higher than embodiment 1 and embodiment 2.
Embodiment 3
With A as raw material (property is shown in Table 1), in paste state bed reactor, with C as catalyst, (property is shown in Table
2), material flow figure is as shown in Figure 2.
It is 200-240 mesh to grind and control particle diameter by sieve method catalyst, with fresh feed weight of oil
6.0 weight % add in paste state bed reactor 1 with raw material and hydrogen from bottom to top.Control slurry
Bed reactor 1 operating condition be：400 DEG C of temperature, pressure 10MPa, hydrogen to oil volume ratio 1000 are empty
Fast 0.2h-1.The conversion level of 1 outlet material of paste state bed reactor is as shown in table 3.Material is from slurry bed system
High-pressure separator 2 is entered in reactor 1, the operating condition of high-pressure separator 2 includes 380 DEG C of temperature,
Pressure 10MPa, and control the discharging speed of high-pressure separator so that 2 bottom of high-pressure separator obtains
Heavier feeds account for 28 weight % of paste state bed reactor inlet amount, obtain from the middle part of high-pressure separator 2
The amount of liquid component accounts for 71 weight % of paste state bed reactor inlet amount.
By above-mentioned heavier feeds are into isolated deasphalted oil in solvent deasphalting tower 4 and contain hydrogenation catalyst
The de-oiled asphalt of agent, the operating condition of solvent deasphalting include solvent for pentane, pentane and heavier feeds
Weight ratio is 1：7, tower top temperature is 82 DEG C, and pressure is 2.8MPa, and deasphalted oil is separated with high pressure
The liquid component obtained in the middle part of device 2 is sent in fixed bed reactors 3 together, will be de- containing hydrogenation catalyst
An oil asphalt part is back to paste state bed reactor 1, arranges outside remainder, and capacity of returns is 5.0 weights
Amount %.
The operating condition of fixed bed reactors 3 includes：Pressure is 15MPa, and reaction temperature is 400 DEG C,
Air speed is 0.2h-1, hydrogen to oil volume ratio is 1200；The catalyst loaded in fixed bed reactors 3 is Chang Ling
RDM the and RCS trades mark hydrogenation catalyst of catalyst Co. production is with 1:The hydrogenation catalyst of 1 mixing.
The outlet of a fixed bed reactors 3 resulting material part is back to paste state bed reactor 1, and capacity of returns is 5.0
Weight %, used as product, product yield is as shown in table 3 for remainder.
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported is shown in Table 4.
Embodiment 4
With B as raw material (property is shown in Table 1), in paste state bed reactor, with D as catalyst, (property is shown in Table
2), material flow figure is as shown in Figure 2.
It is 180-200 mesh to grind and control particle diameter by sieve method catalyst, with fresh feed weight of oil
8.0 weight % add in paste state bed reactor 1 with raw material and hydrogen from bottom to top.Control slurry
Bed reactor 1 operating condition be：370 DEG C of temperature, pressure 16MPa, hydrogen to oil volume ratio 1200 are empty
Fast 0.15h-1.The conversion level of 1 outlet material of paste state bed reactor is as shown in table 3.Material is from slurry bed system
High-pressure separator 2 is entered in reactor 1, the operating condition of high-pressure separator 2 includes 380 DEG C of temperature,
Pressure 10MPa, and control the discharging speed of high-pressure separator so that 2 bottom of high-pressure separator obtains
Heavier feeds account for 29 weight % of paste state bed reactor inlet amount, obtain from the middle part of high-pressure separator 2
The amount of liquid component accounts for 70 weight % of paste state bed reactor inlet amount.
By above-mentioned heavier feeds are into isolated deasphalted oil in solvent deasphalting tower 4 and contain hydrogenation catalyst
The de-oiled asphalt of agent, the operating condition of solvent deasphalting include solvent for hexane, hexane and heavier feeds
Weight ratio is 1：6, tower top temperature is 70 DEG C, and pressure is 3.9MPa, and deasphalted oil is separated with high pressure
The liquid component obtained in the middle part of device 2 is sent in fixed bed reactors 3 together, will be de- containing hydrogenation catalyst
An oil asphalt part is back to paste state bed reactor 1, arranges outside remainder, and capacity of returns is 3.0 weights
Amount %.
The operating condition of fixed bed reactors 3 includes：Pressure is 16MPa, and reaction temperature is 390 DEG C,
Air speed is 0.15h-1, hydrogen to oil volume ratio is 900；The catalyst loaded in fixed bed reactors 3 is Chang Ling
The hydrogenation catalyst of the RDM trades mark of catalyst Co. production.Fixed bed reactors 3 export resulting material
A part is back to paste state bed reactor 1, and capacity of returns is 7 weight %, and remainder is used as product, product
Product yield is as shown in table 3.
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported is shown in Table 4.
Comparative example 3
Method according to embodiment 4 is carried out, except that, the control operation in paste state bed reactor 1
Condition be 450 DEG C of temperature, pressure 15MPa, hydrogen to oil volume ratio 2000, air speed 0.1h-1。
The property of the liquid material that paste state bed reactor 1 is exported and fixed bed reactors 3 are exported, conversion are deep
Degree and product yield are shown in Table 4.As can be seen from Table 4, the toluene insoluble of the outlet of paste state bed reactor 1
The content of thing is apparently higher than embodiment 3 and embodiment 4.
Table 3
Table 4
Inferior heavy oil and/or poor residuum using the present invention can be seen that by embodiment and comparative example
Processing method, can effectively alleviate the problem of paste state bed reactor coking, obtain quality preferably light
Matter oil product.In addition, adding through verification experimental verification, inferior heavy oil of the invention and/or poor residuum
Work method, the operation cycle of fixed bed reactors can reach 1 year more than half, and according to prior art
The processing method of inferior heavy oil and/or poor residuum, the operation cycle of fixed bed reactors are generally left in 1 year
It is right.
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited to above-mentioned
Detail in embodiment, in the range of the technology design of the present invention, can be to the skill of the present invention
Art scheme carries out various simple variants, and these simple variants belong to protection scope of the present invention.
Claims (10)
1. the processing method of a kind of inferior heavy oil and/or poor residuum, the method include inferior heavy oil and
/ or poor residuum send into paste state bed reactor in contact with hydrogenation catalyst, carry out the first hydrogenation reaction, so
Afterwards the first hydrogenation reaction products therefrom is sent in high-pressure separator and is separated, from the top of high-pressure separator
Portion obtains that hydrogen-containing gas, middle part obtain liquid component and bottom obtains the heavy thing containing hydrogenation catalyst
The heavier feeds containing hydrogenation catalyst are carried out solvent deasphalting by material, obtain deasphalted oil and contain adding
The de-oiled asphalt of hydrogen catalyst, and the liquid component and deasphalted oil are sent in fixed bed reactors
The second hydrogenation reaction of row, the condition of first hydrogenation reaction cause turning for inferior heavy oil and/or poor residuum
Change depth and be less than 50%.
2. processing method according to claim 1, wherein, the condition of first hydrogenation reaction
So that the conversion level of inferior heavy oil and/or poor residuum is 20-50%.
3. processing method according to claim 1 and 2, wherein, the processing method also includes
The de-oiled asphalt is at least partly back to into paste state bed reactor.
4. processing method according to claim 3, wherein, it is back to the institute of paste state bed reactor
The amount for stating de-oiled asphalt accounts for 0.5-20 weight % that paste state bed reactor feeds total amount, preferably 1-15 weights
Amount %, more preferably 1-5 weight %.
5. the processing method according to any one in claim 1-4, wherein, the processing side
Method also includes for fixed bed reactors outlet resulting material being at least partly back to paste state bed reactor；It is preferred that
Ground, being back to the amount of the fixed bed reactors outlet resulting material of paste state bed reactor, to account for slurry bed system anti-
Device is answered to feed 1-20 weight % of total amount, preferably 1-15 weight %.
6. processing method according to claim 1 and 2, wherein, the paste state bed reactor
Operating condition includes temperature for 330-420 DEG C, and hydrogen dividing potential drop is 6-25MPa, and hydrogen to oil volume ratio is
100-10000, liquid hourly space velocity (LHSV) are 0.1-0.5h-1；The addition of hydrogenation catalyst is 1-10wt%.
7. the processing method according to any one in claim 1-6, wherein, the slurry bed system
The operating condition of reactor includes temperature for 350-420 DEG C, and hydrogen dividing potential drop is 10-20MPa, hydrogen oil volume
Than for 200-5000, liquid hourly space velocity (LHSV) is 0.1-0.3h-1；The addition of hydrogenation catalyst is 2-8wt%.
8. the processing method according to any one in claim 1-7, wherein, the high pressure point
Include temperature for 350-420 DEG C from the operating condition of device, pressure is 6-16MPa.
9. the processing method according to any one in claim 1-8, wherein, the fixed bed
The operating condition of reactor includes that pressure is 7-22MPa, and reaction temperature is 350-450 DEG C, liquid hourly space velocity (LHSV)
For 0.1-0.5h-1, hydrogen to oil volume ratio is 350-2000.
10. the processing method according to any one in claim 1-9, wherein, the slag inferior
In oil and/or inferior heavy oil, tenor is at least 110 μ g/g, and carbon residue content is at least 10wt%.
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| CN103540353A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Combined hydrogenation process method for treating coal tar and residual oil |
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| CN115261067A (en) * | 2021-04-30 | 2022-11-01 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
| CN115261067B (en) * | 2021-04-30 | 2024-01-09 | 中国石油化工股份有限公司 | Residual oil hydrogenation method |
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