CN103059979A - Fixed bed heavy oil hydrogenation method - Google Patents
Fixed bed heavy oil hydrogenation method Download PDFInfo
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Abstract
The invention discloses a fixed bed heavy oil hydrogenation method. The method comprises: mixing a heavy oil raw material with hydrogen, then passing them through a pretreatment section in an up-flow mode to undergo a pre-hydrogenation reaction under hydrotreating conditions, and then passing the product through a hydrodemetallization reaction section, a hydrodesulfurization reaction section and a hydro-denitrification reaction section in order. Specifically, two solid matters of different specifications are filled in the pretreatment reaction section, and include metal cages for keeping a fixed bed and a particulate catalyst positioned in the space formed by the metal cages. The method provided in the invention uses the technological characteristics of fixed bed hydrogenation and ebullated bed hydrogenation for reference at the same time. The filling mode adopted in the pretreatment reaction section provides greater porosity than the prior art, enhances the dirt-holding capacity and hydrogenation performance of the catalyst bed, and delays the appearance of up-flow reactor hot spots, thus ensuring stable running of the device.
Description
Technical field
The present invention relates to a kind of fixed bed heavy-oil hydrogenation method, particularly take heavy oil as raw material, adopt the multistage hydrogenation technique that pretreatment reaction section and catalyzer grading loading are set to carry out the technological process of heavy oil modification.
Background technology
Fast development along with global economy, the rapid growth of lightweight, clean fuel oil demand and former oil quality are worse and worse, restructuring minute content is more and more higher, how effectively to utilize non-renewable petroleum resources, realize to greatest extent lighting of residual oil, production high value petroleum products is the current important topic that faces.
In order to realize the deep processing of heavy oil, full-bodied inferior raw material is processed into high value added product, so that the heavy-oil hydrogenation technology is developed rapidly.The heavy-oil hydrogenation technology of comparative maturity is the fixed bed residual hydrogenation at present, and this technological operation is steady, at home and abroad is used widely.Conventional heavy oil fixed bed hydrogenating technique adopts a plurality of reactors in series usually; load successively protective material, hydrodemetallation (HDM) agent, hydrogen desulfurization agent and hydrodenitrogenation catalyst in the reactor; according to the filling order of catalyzer in reactor; the particle size of catalyzer reduces successively; surface-area increases successively; the shared total pore volume of catalyzer macropore reduces successively, and active metallic content increases successively.Usually adopt this catalyst grade to join the filling scheme processing heavy oil, carry out successively hydrogenation detergency (metallic salt that iron, calcium and sodium salt etc. easily remove), hydrodemetallation (HDM) (being mainly nickel and vanadium), hydrogenating desulfurization and hydrodenitrification and hydroconversion reactions, for the FCC apparatus in downstream provides the high-quality charging.But because raw material in poor quality trend is more and more serious, viscosity and the foreign matter content of raw material are more and more higher, so that usually only can maintain about 1 year the running period of whole device.Although France Inst Francais Du Petrole proposes guard reactor and adopts the operating method switched can the proper extension operational cycle; but because the catalyst activity of guard reactor filling is low; the load of the catalyst hydrogenation removing impurities matter in the subsequent reactor does not alleviate, so the processing property of whole reactive system fails significantly to improve.
CN1197105A discloses a kind of method of hydrocarbon raw material of hydrotreatment containing metal pollutent, and the method is in the presence of hydrogen, and raw material is contacted with one or more beds in the first catalyzer, the second catalyzer, the 3rd catalyzer.Various catalyst properties, function is different.In fact, along the logistics direction, catalyst activity becomes greatly gradually, and the aperture reduces gradually, is first demetalization, the again desulfurization of standard, the hydrotreatment process of last denitrogenation.The protective material that uses in this technology is conventional fixed bed protective material, and activity is lower, can not effectively improve the Hydrogenation of whole grating catalyst system.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of fixed bed heavy oil hydrogenation process, a pretreatment section especially is set, the solid matter of two kinds of different sizes of this section filling, the metal cage and the microgranular catalyzer that keep fixed bed, described microgranular catalyzer are positioned in the space of metal cage formation.This pretreatment section has the operating features of fixed bed and ebullated bed simultaneously concurrently, larger appearance dirt ability and hydrogenation removing impurities matter and asphaltenes conversion ability is provided, thereby can guarantees that subsequent catalyst has comparatively elastic operating space, the long-term operation of implement device.
A kind of fixed bed heavy-oil hydrogenation method of the present invention comprises following content:
(a) heavy oil feedstock and hydrogen are mixed into pretreatment section, carry out the pre-hydrotreating reactions such as detergency, partial hydrogenation demetalization and asphaltenes conversion;
(b) the pretreatment section reaction effluent enters the hydrodemetallation (HDM) conversion zone, reacts under the hydrodemetallation (HDM) condition;
(c) the hydrodemetallation (HDM) reaction effluent enters the hydrodesulfurization reaction section, reacts under hydrodesulfurizationconditions conditions;
(d) the hydrodesulfurization reaction effluent enters the hydrodenitrification conversion zone, reacts under the hydrodenitrification condition;
(e) logistics obtains light ends oil and hydrogenation tail oil through the water distilling apparatus fractionation after the reaction of step (d) gained.
Wherein the said pretreatment section of step (a) comprises the solid matter of two kinds of different sizes, and a kind of for keeping the large size inertia cage of fixed bed, the material of cage shape thing is generally metal material.Described metal cage is preferably the multiaspect cage of the face with 4 above homalographics or unequal-area, and each face of cage all has aperture, and pitch of holes is 0.1～2 mm, and the diameter of its mesopore is all less than the diameter of microgranular catalyzer.Described microgranular catalyzer is wrapped in the metal cage, and its particle diameter (spherical diameter or bar shaped diameter) is 0.2～3mm, and specific surface area is 100～300m
2/ g.Wherein metal cage is 10～1000 with the equivalent diameter ratio of particle catalyst.Metal cage in the reactor mainly plays and supports and buffer action, is used for the dispersion of particle catalyst, the distribution of gas-liquid logistics, and the transmission of reaction heat is for active catalyst forms a plurality of little boiling spaces.For each fixing reactor, the structure of metal cage and size are fixing and uniform.
Microgranular catalyzer recited above, its carrier can be in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more, reactive metal can be in nickel, cobalt, molybdenum or the tungsten one or more.Can comprise by weight percentage such as the catalyzer composition: nickel or cobalt count 1%～25% with oxide compound, and molybdenum or tungsten count 1%～30% with oxide compound.The shape of catalyzer is extrudate or sphere, and bulk density is 0.4～0.9g/cm
3, particle diameter (spherical diameter or bar shaped diameter) is 0.2～3mm, specific surface area is 100～300m
2/ g.Wherein the large size metal cage is 10～1000 with the equivalent diameter ratio of granules of catalyst.The large size metal cage mainly plays and supports and buffer action, is used for the dispersion of tiny catalyzer, the distribution of gas-liquid logistics, and the transmission of reaction heat forms the space of a plurality of little random motions for catalyzer.
In pretreatment section, before reactor that metal cage is packed into, at first microgranular catalyzer not being sealed the cage face from a reservation of metal cage joins the cage, the loadings scope of catalyzer is 40%～90% of cage volume in the metal cage, then this cage face of mechanical close for example can be by this cage face of welded closure; The metal cage that particle catalyst will be housed is again packed into the dilute phase type of feed in the reactor.
Described pretreatment operation condition is: reaction pressure 6～20MPa, and temperature of reaction: 350～420 ℃, preferred 370～410 ℃, hydrogen to oil volume ratio 500～3000, volume space velocity is 0.5～3h during liquid
-1
Step (b), (c) and (d) Hydrodemetalation catalyst, Hydrobon catalyst and the hydrodenitrogenation catalyst that use of described process can be with any existing the type catalyzer.This type of catalyzer generally all is as carrier take porous inorganic oxide, the oxide compound of group vib and/or group VIII metal oxide such as W, Mo, Co and Ni etc. is active ingredient, optionally adds the catalyzer of other various auxiliary agents such as P, Si, the elements such as F, B.The FZC catalyst series of for example being produced by catalyzer pilot scale base, Fushun.The normal operating condition of residue fixed-bed hydrodemetallation (HDM), hydrogenating desulfurization and hydrodenitrification is: reaction pressure 10～16MPa, and 340～420 ℃ of temperature of reaction, preferred 360～410 ℃, hydrogen to oil volume ratio 500～2000, volume space velocity is 0.5～1.0h during liquid
-1
Above said pretreatment catalyst, Hydrodemetalation catalyst, Hydrobon catalyst and hydrodenitrogenation catalyst can be seated in one or more reactors.
The described water distilling apparatus of step (e) can comprise the devices such as atmospheric distillation tower and vacuum still.Doing of described light ends oil is generally 330 ℃～385 ℃.Light ends can be used as gasoline or diesel oil blending component usually, and hydrogenation tail oil can be used as the raw material of catalytic cracking unit.
Heavy oil feedstock described in the inventive method can be in viscous crude, long residuum, vacuum residuum, solvent-deasphalted oils, shale oil or the coal tar one or more.
Compared with prior art, the advantage of the inventive method is:
(1) before fixed bed residuum hydrogenating and metal-eliminating, hydrogenating desulfurization and the hydrodenitrification reactor of routine, activity is set higher; the pretreatment catalyst that voidage is large substitutes the SA protective material in original wide aperture; can adjust the Hydrogenation of whole grading loading catalyst system, improve the flexibility of operation of device.
(2) adopt the cage structure that microgranular active catalyst is housed to be used for the residual oil pre-treatment, can guarantee that inner catalyst can be full of whole reaction compartment between wider operational zone, microgranular catalyzer is in the random motion state simultaneously, and high appearance impurity ability is provided.
(3) adopt microgranular catalyzer is packed in the inertia cage structure, then it is packed into and participate in reaction in the reactor, can be according to composition and the reaction characteristics of heavy oil feedstock logistics, adjust the content of the microgranular catalyzer in the cage, thereby adjust the voidage between the correlated response section catalyzer, improve the appearance dirt ability at this place.
(4) adopt the catalyzer of grading loading to be used for residual hydrogenation, logistics property and catalyst performance can be carried out reasonably combinedly, give full play to the activity of catalyzer, assurance quality product.
Description of drawings
Fig. 1 is the schematic flow sheet of fixed bed heavy oil hydrogenation process of the present invention.
Embodiment
The embodiment of this programme is briefly described below in conjunction with the device schema:
Wherein sequence number 1 is head tank, and 2 is the pretreatment reaction device, and 3 is the hydrodemetallation (HDM) reactor, and 4 is hydrodesulphurisatioreactors reactors, 5 hydrodenitrification reactors, and 6 is water distilling apparatus, 7 gasoline, 8 is diesel oil, and 9 is hydrogenation tail oil, and 10 is hydrogen, and all the other are pipeline.
As shown in Figure 1, the principle technique processed of heavy-oil hydrogenation of the present invention is: at first the heavy oil feedstock in the head tank 1 mixes with hydrogen 10 and enters pretreatment reaction device 2 with upflowing and carry out hydrogenation detergency, hydrodemetallation (HDM) and part bituminous matter hydroconversion reactions; Pretreatment stream enters in turn hydrodemetallation (HDM) reactor 3, hydrodesulphurisatioreactors reactors 4 and hydrodenitrification reactor 5 and carries out hydrodemetallation (HDM), hydrogenating desulfurization and hydrodenitrification/hydroconversion reactions; Logistics obtains gasoline fraction 7, diesel oil distillate 8 and hydrogenation tail oil 9 through water distilling apparatus 6 after the reaction.
Pretreatment section among the present invention comprises the solid matter of two kinds of different sizes, and a kind of for keeping the large size inertia cage of fixed bed, the material of cage shape thing is generally metal material.Described metal cage is preferably the multiaspect cage of the face with 4 above homalographics or unequal-area, and each face of cage all has aperture, and pitch of holes is 0.1～2 mm, and the diameter of its mesopore is all less than the diameter of microgranular catalyzer.Described microgranular catalyzer is wrapped in the metal cage, and its particle diameter (spherical diameter or bar shaped diameter) is 0.2～3mm, and specific surface area is 100～300m
2/ g.Wherein metal cage is 10～1000 with the equivalent diameter ratio of particle catalyst.Metal cage in the reactor mainly plays and supports and buffer action, is used for the dispersion of particle catalyst, the distribution of gas-liquid logistics, and the transmission of reaction heat is for active catalyst forms a plurality of little boiling spaces.For each fixing reactor, the structure of metal cage and size are fixing and uniform.
Microgranular catalyzer recited above, its carrier can be in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more, reactive metal can be in nickel, cobalt, molybdenum or the tungsten one or more.Can comprise by weight percentage such as the catalyzer composition: nickel or cobalt count 1%～25% with oxide compound, and molybdenum or tungsten count 1%～30% with oxide compound.The shape of catalyzer is extrudate or sphere, and bulk density is 0.4～0.9g/cm
3, particle diameter (spherical diameter or bar shaped diameter) is 0.2～3mm, specific surface area is 100～300m
2/ g.Wherein the large size metal cage is 10～1000 with the equivalent diameter ratio of granules of catalyst.The large size metal cage mainly plays and supports and buffer action, is used for the dispersion of tiny catalyzer, the distribution of gas-liquid logistics, and the transmission of reaction heat forms the space of a plurality of little random motions for catalyzer.
In pretreatment section, before reactor that metal cage is packed into, at first microgranular catalyzer is not sealed the cage face from a reservation of metal cage and join the cage, the loadings scope of catalyzer is 40%～90% of cage volume in the metal cage.Then this cage face of mechanical close.The metal cage that microgranular catalyzer will be housed is again packed into the dilute phase type of feed in the reactor.
Described pretreatment operation condition is: pressure 6～20MPa, and temperature: 350～420 ℃, preferred 370～410 ℃, hydrogen to oil volume ratio 500～3000, volume space velocity is 0.5～3h during liquid
-1
The available any existing the type catalyzer of hydrodemetallation (HDM) agent of the present invention, hydrogen desulfurization agent and hydrodenitrification agent.This type of catalyzer generally all is as carrier take porous inorganic oxide, the oxide compound of group vib and/or group VIII metal oxide such as W, Mo, Co and Ni etc. is active ingredient, optionally adds the catalyzer of other various auxiliary agents such as P, Si, the elements such as F, B.The FZC series of for example being produced by catalyzer pilot scale base, Fushun weighs, residual oil hydrocatalyst.The normal operating condition of residue fixed-bed hydrodemetallation (HDM), hydrogenating desulfurization and hydrodenitrification is: pressure 10～16MPa, and temperature: 340～420 ℃, preferred 360～410 ℃, hydrogen to oil volume ratio 500～2000, volume space velocity is 0.5～1.0h during liquid
-1
For further specifying all main points of the present invention, enumerate following examples.Catalyzer forms and raw material forms and the character percentage composition is weight percentage.
The feedstock property that test is used is: the content of metallic nickel and vanadium is 100 μ g/g, and calcium contents is 121 μ g/g, and iron and sodium content are 7.6 μ g/g, and asphalt content 3.3wt%, carbon residue content are 10.4wt%, and sulphur content is 2.79%, and nitrogen content is 0.43%.
Embodiment 1
The present embodiment is the hydropyrolysis experiment that fixed bed heavy oil upgrading technique is carried out poor residuum, and the ebullated bed reactor of pre-hydrogenation adopts outside the upflowing operating method, the fixed bed operation mode that all the other each reactors adopt gas and liquid flowing to flow downward.At first the heavy oil feedstock in the head tank 1 mixes with hydrogen 10 and enters pretreatment reaction device 2 with upflowing and carry out hydrogenation detergency, hydrodemetallation (HDM) and part bituminous matter hydroconversion reactions; Pretreatment stream enters in turn hydrodemetallation (HDM) reactor 3, hydrodesulphurisatioreactors reactors 4 and hydrodenitrification reactor 5 and carries out hydrodemetallation (HDM), hydrogenating desulfurization and hydrodenitrification/hydroconversion reactions; Logistics obtains＜7,180～350 ℃ of diesel oil distillate 8 Hes of 180 ℃ of gasoline fractions through water distilling apparatus 6 after the reaction〉350 ℃ of hydrogenation tail oils 9.Wherein the microgranular catalyzer that uses of pretreatment section as microspheroidal with the molybdenum-nickel catalyzator of aluminum oxide as carrier, wherein contain MoO in the catalyzer
3Be 9wt%, containing NiO is 3.5wt%.The bulk density of catalyzer is 0.69g/cm
3, surface-area is 220m
2/ g, the granules of catalyst mean diameter is 1mm, the equivalent diameter of metal cage and catalyzer is than 80, for catalyst loading volume in each inertia cage accounts for 60% of cage volume.Hydrodemetallation (HDM) reactor charge FZC-202 catalyzer, hydrodesulphurisatioreactors reactors filling FZC-34 catalyzer, hydrodenitrification reactor charge FZC-41 catalyzer.
Reaction conditions and test-results are listed in respectively table 1.Each reactor all can keep the running period grown.
The test operation process of the present embodiment is substantially the same manner as Example 1, and difference is that the microgranular catalyzer that loads the inertia cage of the conversion zone from the logistics entrance to distance entrance 1/3rd in the pretreatment reaction device contains MoO
3Be 6wt%, containing NiO is 1.2wt%, and bulk density is 0.65g/cm
3, surface-area is 190m
2/ g, the granules of catalyst mean diameter is 1.5mm, it accounts for 40% of cage volume; Metal cage is 60 with the equivalent diameter ratio of catalyzer; Contain MoO in the catalyzer of residue conversion zone filling
3Be 12wt%, containing NiO is 4wt%.Catalyst bulk density is 0.71g/cm
3, surface-area is 230m
2/ g, the granules of catalyst mean diameter is 0.8mm, and it accounts for 70% of cage volume, and metal cage is 100 with the equivalent diameter ratio of catalyzer.Reaction conditions and test-results see Table 1.
Comparative example
Comparative example adopts the grading loading mode of conventional fixed bed residual oil hydrocatalyst, and wherein pretreatment section is loaded protective material FZC-101, and all the other are substantially the same manner as Example 1.Reaction conditions and test-results see Table 1.
Table 1 reaction conditions and result
| Numbering | Embodiment 1 | |
Comparative example |
| Pre-hydrotreating reaction | ? | ? | ? |
| Temperature, ℃ | 375 | 373 | 380 |
| Pressure, MPa | 15.7 | 15.7 | 15.7 |
| Hydrogen-oil ratio, v/v | 600 | 600 | 600 |
| Air speed, h -1 | 0.8 | 1.0 | 0.8 |
| The hydrodemetallation (HDM) reaction | ? | ? | ? |
| Temperature, ℃ | 378 | 375 | 380 |
| Pressure, MPa | 15.7 | 15.7 | 15.7 |
| Hydrogen-oil ratio, v/v | 600 | 600 | 600 |
| Air speed, h -1 | 0.8 | 0.8 | 0.8 |
| Hydrodesulfurization reaction | ? | ? | ? |
| Temperature, ℃ | 378 | 375 | 380 |
| Pressure, MPa | 15.7 | 15.7 | 15.7 |
| Hydrogen-oil ratio, v/v | 600 | 600 | 600 |
| Air speed, h －1 | 0.8 | 0.8 | 0.8 |
| The hydrodenitrification reaction | ? | ? | ? |
| Temperature, ℃ | 376 | 375 | 380 |
| Pressure, MPa | 15.7 | 15.7 | 15.7 |
| Hydrogen-oil ratio, v/v | 600 | 600 | 600 |
| Hydrogen-oil ratio, v/v | 600 | 600 | 600 |
| Air speed, h -1 | 0.8 | 0.8 | 0.8 |
| Test-results: | ? | ? | ? |
| Desulfurization degree, % | 92.4 | 93.8 | 89.5 |
| Denitrification percent, % | 63.2 | 67.4 | 62.1 |
| Demetallization per, % | 95.6 | 96.2 | 89.7 |
Adopt catalyst loading pattern of the present invention to process inferior raw material, demetalization under relatively mitigation condition, desulfurization and denitrification percent all are better than conventional heavy oil fixed bed reaction result, through the long-term operation result as can be known, adopt catalyst grade prescription formula of the present invention the appearance metal ability of catalyzer can be improved 20 to 50 percentage points.
Claims (11)
1. fixed bed heavy-oil hydrogenation method comprises following content:
(a) heavy oil feedstock and hydrogen are mixed into pretreatment section, under the hydrogenation pretreatment condition, carry out pre-hydrotreating reaction; Wherein said pretreatment section comprises the solid matter of two kinds of different sizes, and a kind of for keeping the large size metal cage of fixed bed, another kind of for being wrapped in the particle catalyst in the metal cage, metal cage is 10～1000 with the equivalent diameter ratio of particle catalyst;
(b) step (a) gained pretreatment section reaction effluent enters the hydrodemetallation (HDM) conversion zone, reacts under the hydrodemetallation (HDM) condition;
(c) step (b) gained hydrodemetallation (HDM) reaction effluent enters the hydrodesulfurization reaction section, reacts under hydrodesulfurizationconditions conditions;
(d) step (c) gained hydrodesulfurization reaction effluent enters the hydrodenitrification conversion zone, reacts under the hydrodenitrification condition;
(e) logistics obtains light ends oil and hydrogenation tail oil through the water distilling apparatus fractionation after the reaction of step (d) gained.
2. in accordance with the method for claim 1, it is characterized in that, described metal cage is the multiaspect cage with face of 4 above homalographics or unequal-area, and each face of cage all has aperture, pitch of holes is 0.1～2 mm, and the diameter of its mesopore is all less than the diameter of microgranular catalyzer.
3. in accordance with the method for claim 1, it is characterized in that, described metal cage is Rotating Stainless Steel Cage.
4. in accordance with the method for claim 1, it is characterized in that, the particle diameter of described microgranular catalyzer is 0.2～3mm, and specific surface area is 100～300m
2/ g.
5. in accordance with the method for claim 1, it is characterized in that, the carrier of described microgranular catalyzer is one or more in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide, reactive metal is one or more in nickel, cobalt, molybdenum or the tungsten, catalyzer forms and comprises by weight percentage, nickel or cobalt count 1%～25% with oxide compound, and molybdenum or tungsten count 1%～30% with oxide compound.
6. in accordance with the method for claim 1, it is characterized in that, in the described pretreatment section of step (a), the loadings scope of catalyzer is 40%～90% of metal cage volume in the metal cage.
7. in accordance with the method for claim 1, it is characterized in that, the described pretreatment operation condition of step (a) is: reaction pressure 6～20MPa, and 350～420 ℃ of temperature of reaction, hydrogen to oil volume ratio 500～3000, volume space velocity is 0.5～3h during liquid
-1
8. in accordance with the method for claim 1, it is characterized in that, the described hydrodemetallation (HDM) condition of step (b), (c) or (d) operational condition of residue fixed-bed hydrodemetallation (HDM), hydrogenating desulfurization and hydrodenitrification be: pressure 10～16MPa, 340～420 ℃ of temperature, hydrogen to oil volume ratio 500～2000, volume space velocity is 0.5～1.0h during liquid
-1
9. in accordance with the method for claim 1, it is characterized in that, described pretreatment catalyst, hydrodemetallation (HDM) agent, hydrogen desulfurization agent and hydrodenitrification agent are seated in one or more reactors.
10. in accordance with the method for claim 1, it is characterized in that, described heavy oil feedstock is one or more in viscous crude, long residuum, vacuum residuum, solvent-deasphalted oils, shale oil or the coal tar.
11. in accordance with the method for claim 1, it is characterized in that, the described water distilling apparatus of step (e) comprises the devices such as atmospheric distillation tower and vacuum still, and doing of described light ends oil is 330 ℃～385 ℃.
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| CN105316041A (en) * | 2014-07-30 | 2016-02-10 | 中国石化工程建设有限公司 | Residual oil hydrogenation method |
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| CA2314033A1 (en) * | 1999-07-21 | 2001-01-21 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Process for hydrocracking of petroleum heavy oil |
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2011
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| EP0098289A1 (en) * | 1982-01-07 | 1984-01-18 | University Patents, Inc. | Heterocatalyst system |
| CA2314033A1 (en) * | 1999-07-21 | 2001-01-21 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Process for hydrocracking of petroleum heavy oil |
| US20100155293A1 (en) * | 2008-12-18 | 2010-06-24 | Ifp | Hydrocracking process including switchable reactors with feedstocks containing 200 ppm by weight - 2% by weight of asphaltenes |
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| CN105316041A (en) * | 2014-07-30 | 2016-02-10 | 中国石化工程建设有限公司 | Residual oil hydrogenation method |
| CN105316041B (en) * | 2014-07-30 | 2018-04-10 | 中国石化工程建设有限公司 | A kind of residual hydrogenation method |
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