CN102453543B - Combined process of hydrotreatment and catalytic cracking for residuum - Google Patents
Combined process of hydrotreatment and catalytic cracking for residuum Download PDFInfo
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Abstract
The invention discloses a combined process of hydrotreatment and catalytic cracking for residuum. According to the process, a boiling bed hydrotreatment method is used in hydrotreatment of residuum, and the process comprises the following steps that: liquid phase products obtained after the raw material of residuum undergoes boiling bed hydrotreatment are subjected to fractional distillation so as to obtain light components and heavy components; the light components are used as first-stage charging materials and enter into a catalytic cracking riser reactor from the bottom of the reactor; the heavy components directly enter into a catalytic cracking fractionator and are subjected to fractional distillation together with effluent of a catalytic cracking reaction so as to isolate dry gas, liquefied gas, gasoline fraction, diesel oil fraction, recycle oil and slurry oil, wherein, the recycle oil is used as a second-stage charging material of the riser reactor, and the slurry oil is used as a charging component for delayed coking. Compared to the prior art, the process provided in the invention has the following characteristics: gasoline with a high octane number, diesel oil fraction and liquefied gas with a high added value can be produced; reaction thermal energy is fully utilized, thereby reducing energy consumption in production.
Description
Technical field
The present invention relates to a kind of residual oil weight-lightening method, specifically by residual hydrocracking and catalytic cracking organic assembling, the processing method of mainly producing high octane gasoline products and diesel oil distillate as raw material take residual oil.
Background technology
Along with crude oil day by day becomes heavy, becomes bad, increasing residual oil needs processing treatment.Processing treatment heavy, residual oil will be not only lower boiling product by its cracking, as petroleum naphtha, intermediate oil and pressure reduction gas wet goods, but also will improve their hydrogen-carbon ratio, and this just need to realize by the method for decarburization or hydrogenation.Wherein decarbonization process comprises coking, solvent deasphalting, heavy oil fluid catalytic cracking etc.; Hydrogenation comprises hydrocracking, hydrofining etc.Hydrogenation method can hydrocracking residual oil, improves the productive rate of liquid product, and can also remove heteroatoms wherein, is conducive to improve the quality of product.But hydrogenation method is catalysis complete processing, there is hydrogenation catalyst inactivation problem, when especially processing poor quality, heavier hydrocarbon feeds, Catalysts Deactivation Problems is more serious.At present, in order to reduce the cost of heavy, poor residuum processing, increase oil refining enterprise's profit, the technique of processing heavy, poor residuum is still take decarbonization process as main, but its poor product quality need to be carried out aftertreatment and could be utilized, wherein deasphalted oil and wax tailings cut especially need to carry out hydrotreatment, could continue to use the lighting devices such as catalytic cracking or hydrocracking to process, therefore, each oil refining enterprise all separately has the hydrotreater of deasphalted oil and wax tailings.
The slag oil cracking rate of residual hydrocracking technology is lower, and main purpose is to supply raw materials as the device such as catalytic cracking or coking for downstream raw material lighting device.By hydrotreatment, sulphur, nitrogen, metal impurities content and carbon residue in poor residuum are obviously reduced, thereby obtain the charging that lighting device in downstream can be accepted, especially catalytic cracking unit, therefore at present in heavy, residual hydrogenation modifying process technology take residue fixed-bed hydrotreatment and catalytic cracking combination technique as mainstream technology.
Existing residual hydrocracking and catalytic cracking combined technique, first be that residual oil is carried out to hydrotreatment, hydrogenated oil is isolated petroleum naphtha and diesel oil distillate, hydrogenation tail oil is as heavy oil fluid catalytic cracking charging, carry out catalytic cracking reaction, product is dry gas, liquefied gas, gasoline, diesel oil and coke, and recycle stock carries out catalysis freshening or loop back residual hydrogenation equipment mixing and carrying out hydrotreatment with residual hydrocracking raw material, and catalytic slurry gets rid of outward or partially catalyzed freshening or loop back residual hydrogenation equipment.The unfavorable factors such as above-mentioned residual hydrocracking and catalytic cracking combined technique exist yield of gasoline low, and heat energy loss is large, facility investment height.
And wide for the boiling bed hydrogenation technology adaptability to raw material of heavy oil upgrading, can process various poor residuum raw materials, not restricted by feedstock property, but with fixed bed comparatively speaking, its impurity removal percentage is lower, degree of saturation is poor.Boiling bed hydrogenation is processed and is generated oil conventionally using wax oil cut as catalytically cracked material, and heavy oil carries out respectively processing treatment as delayed coking raw material, obtains corresponding gasoline, diesel oil distillate, needs kinds of processes to combine.
US 6447671 discloses a kind of combination process process for heavily residuum hydroconversion.Detailed process is: heavy residual oil raw material and hydrogen are mixed into boiling bed hydrogenation cracking reaction district, after hydrocracking reaction, logistics obtains lighting end and last running through tripping device, and lighting end enters distillate fixed bed hydrogenation processing section or directly enters water distilling apparatus carries out narrow fraction cutting; Heavy constituent after filtration system enters heavy oil fixed bed hydrogenating reaction zone after removing catalyst solid residue; Or the whole logistics that flow out from boiling bed hydrogenation cracking reaction district directly enter filtering system, enter heavy oil fixed bed hydrogenating processing reaction district after isolating catalyst solid material; Reacted all or part of logistics enters water distilling apparatus, cuts out each lighting end and heavy constituent, and the heavy constituent wherein obtaining enters catalytic cracking unit or loops back heavy-oil hydrogenation and processes or hydrocracking reaction district.This combination process process just requires according to the charging of device and reacted logistics property carries out the rational Match of processing means, the feature of each COMBINED PROCESS is not given full play of.
US 6277270 has introduced and has used fixed bed hydrogenation, boiling bed hydrogenation and catalytic cracking combined technique to process the technological process of heavy crude hydrocarbon feed.Process description: residual oil raw material obtains decompressed wax oil and vacuum residuum through underpressure distillation, wherein all or part of fixed bed hydrogenation treatment unit that enters of decompressed wax oil reacts, and hydrogenation wax oil obtains distillate and hydrogenation tail oil (a) through air distillation; Wherein vacuum residuum directly or be mixed into fluidized bed device with part decompressed wax oil and carry out hydrocracking reaction, generate oil and obtain atmospheric distillate and long residuum (b) through air distillation, wherein atmospheric distillate enters fixed bed hydrogenation reactor and carries out hydrogenation reaction, long residuum (b) enters boiling bed hydrogenation device, or as oil fuel remover etc.This combination process just requires to carry out the use of combining of device according to the liquid feeding of different device, not specifically in conjunction with polytechnic feature, bring into play the sharpest edges of each technique as far as possible.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of residual hydrocracking and catalytic cracking combination process, the method can maximum be produced gasoline and diesel product, and technological process is simple simultaneously, and overall energy consumption is low.
Residual hydrocracking of the present invention and catalytic cracking combination process, wherein catalytic cracking adopts riser reactor, described riser reactor arranges two-stage opening for feed, wherein first step opening for feed is arranged on the bottom of riser tube, second stage opening for feed is above first step opening for feed, and residual hydrocracking adopts boiling bed residual oil hydroprocessing technique, the method comprises: residual oil raw material enters boiling bed hydrogenation treatment reactor, under hydrogen and hydrotreating catalyst existence, carry out hydrogenation reaction, hydrogenation reaction effluent gas-liquid separation, liquid phase fractionates out light constituent and heavy constituent, and wherein the cut point of light constituent and heavy constituent is 320～380 ℃, as the catalytic cracking riser reactor first step, charging enters reactor by first step opening for feed to light constituent, heavy constituent enters separation column by the bottom of catalytic cracking fractionating tower, the entry position that heavy constituent enters catalytic cracking fractionating tower catalytic cracking reaction effluent enter catalytic cracking fractionating tower entry position above, heavy constituent and catalytic cracking reaction effluent are through fractionation, isolate dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil, wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage, enter reactor by second stage opening for feed, carry out catalytic cracking reaction.
In the inventive method, slurry oil can be used as delayed coking feed component, processes to coker.
The reactor of described catalytic cracking unit adopts riser reactor, this reactor arranges two-stage opening for feed, wherein first step opening for feed is arranged on the bottom of reactor, it can be charging place of conventional riser reactor, also can be arranged on as requested any position of riser tube bottom, second stage opening for feed is arranged on the top of first step opening for feed, accounts for 1/30～1/5 of whole riser tube height apart from the distance of first step opening for feed, is preferably 1/10～1/6.This technical process is specially: light constituent injects from the first step opening for feed of riser reactor bottom as first step charging, contact with the high-temperature regenerated catalyst from revivifier, the oil gas that cracking reaction generates and the catalyst mixture of deposit coke move up along riser reactor, the recycle stock entering with the second stage opening for feed from riser reactor mixes, and carries out catalytic cracking reaction.
In the inventive method, residual oil raw material comprises long residuum or vacuum residuum or poor residuum, can be also the residual oil raw material in other source, also can contain one or several in part wax tailings, deasphalted oil, heavy distillate in residual oil raw material simultaneously.First hydrogenation reaction effluent carries out gas-liquid separation, this gas-liquid separation is carried out under the condition identical with reaction pressure grade, the gas phase that separation obtains is mainly hydrogen, after selectable depriving hydrogen sulphide is processed, be cycled to used in hydrogenation reaction, hydrogenation process needs to supplement the consumption of new hydrogen with postreaction process simultaneously.The liquid phase obtaining after hydrogenation reaction effluent gas-liquid separation enters separation column, isolates light constituent and heavy constituent; Wherein light constituent enters riser reactor by catalytic cracking riser bottom, heavy constituent directly enters catalytic cracking fractionating tower bottom, carry out fractionation together with catalytic cracking reaction effluent, obtain dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil, wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage, enter reactor by second stage opening for feed, carry out catalytic cracking reaction.
In the present invention, the boiling bed hydrogenation catalyst that described boiling bed residual oil hydroprocessing technique adopts is the hydrotreating catalyst of this area routine, and wherein the active metal of catalyzer can be one or more in nickel, cobalt, molybdenum or tungsten.As catalyzer composition can comprise by weight percentage: nickel or cobalt are 1%～20% (calculating by its oxide compound), molybdenum or tungsten are 1%～30% (calculating by its oxide compound), and carrier can be one or more in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or titanium oxide.The shape of catalyzer is extrudate or spherical, and bulk density is 0.4～0.9g/cm
3, particle diameter (spherical diameter or bar shaped diameter) is 0.08～1.2mm, specific surface area is 100～300m
2/ g.The operational condition of boiling bed hydrogenation processing is generally: reaction pressure 6～30MPa, 400～490 ℃ of temperature of reaction, volume space velocity 0.1～5.0h when liquid
-1, hydrogen to oil volume ratio (under standard conditions) 200～2000; Preferred operational condition is: reaction pressure 15～20MPa, 420～470 ℃ of temperature of reaction, volume space velocity 0.5～2.0h when liquid
-1; Hydrogen to oil volume ratio (under standard conditions) 400～1000.Described reaction product tripping device can be high-pressure separator or flashing tower, and the temperature of cutting apart of light constituent and heavy constituent is 320～380 ℃, and light constituent mainly comprises gasoline fraction and diesel oil distillate.
The present invention is applicable to normal pressure or vacuum residuum hydrotreatment, is particularly useful for the hydrocracking of heavy hydrocarbon.The actual conditions of residual hydrocracking process can specifically be determined according to the requirement of the character of raw material and catalytic cracking unit charging.
In the inventive method, catalytic cracking can adopt this area routine techniques.Catalytic cracking unit can be a set of or a set of more than, every covering device at least should comprise a reactor, a revivifier.Catalytic cracking unit arranges separation column, can every cover catalytic cracking unit set respectively, also can share.Catalytic cracking fractionating tower is dry gas, liquefied gas, gasoline, diesel oil distillate, recycle stock and slurry oil by the fractionation of catalytic cracking reaction effluent.
In the inventive method, catalytic cracking unit operates by this area general condition: temperature of reaction is 450～600 ℃, preferably 480～550 ℃; Regeneration temperature is 600～800 ℃, is preferably 650～750 ℃, and agent weight of oil is than 2～30, preferably 4～10; With 0.1～15.0 second duration of contact of catalyzer, best 0.5～5.0 second; Pressure 0.1～0.5MPa.The catalytic cracking catalyst adopting comprises the catalyzer that is generally used for catalytic cracking, as silica-alumina catalyst, silica-magnesia catalyst, acid-treated carclazyte and X-type, Y type, ZSM-5, M type, layer post equimolecular sieve cracking catalyst, preferably molecular sieve cracking catalyst, this is because the activity of molecular sieve cracking catalyst is high, green coke is few, gasoline yield is high, and transformation efficiency is high.
In the inventive method, the concrete operations condition of residual hydrocracking and catalytic cracking can be obtained by simple experiment according to feedstock property and product quality indicator by technician.
The invention has the advantages that:
1, in whole combination process, the light constituent that boiling bed residual oil hydrogenation process generates, as the charging of the catalytic cracking riser first step, after reacting with high-temperature regenerated catalyst short-time contact, arrive rapidly riser tube second stage charging place, obtain cooling to a certain extent at this, stoped the generation of secondary reaction, gasoline yield is maximized.
2, the feedstock property of boiling bed hydrogenation processing is poor, and the boiling bed hydrogenation degree of depth relaxes in addition, and transformation efficiency is lower, and tail oil character is poor, the catalytically cracked material that has not been.The heavy constituent that boiling bed hydrogenation process obtains directly enters catalytic cracking fractionating tower and carries out fractionation, this heavy constituent can fractionate out wax oil and heavy oil, wherein wax oil is included in recycle stock, enter catalytic cracking unit by riser tube second stage opening for feed, effectively utilize catalytic cracking process feature, maximum is produced light ends oil; Heavy oil is included in slurry oil, and as coking raw material component, to coker processing, the coking raw material of poor residuum, is good feed composition relatively.
3, from whole combination process, in hydrotreater, only simple and easy fractionating system need be set, hydrotreatment generates oil and directly enters catalyst cracker and separation column, do not need to establish fresh feed pump, a large amount of heat-exchange equipments have been reduced simultaneously, greatly reduce the loss of heat, greatly reduced the required energy of fractionation process simultaneously, thereby reduced the energy consumption of whole technological process.
4, the position that hydrogenation heavy constituent enters catalytic cracking fractionating tower is arranged on the top of catalytic cracking reaction effluent entrance, is conducive to like this catalysis and generates oil and carry out heat exchange with heavy constituent, is conducive to the separation of light constituent.
5, catalytic cracking of the present invention adopts two-stage charging, and wherein the light constituent in hydrogenated oil enters reactor as first step charging by riser tube bottom, contacts with high-temperature regenerated catalyst, generates stop bracket gasoline and liquefied gas.After the charging of the riser tube first step and catalyst reaction, the rapid desorption of reaction product, together enters air-flow with the catalyzer (catalyst activity at this moment slightly declines) that has part of coke; After second stage charging is injected, contact with the catalyzer from the first step, under the condition relatively relaxing, carry out catalytic cracking reaction, generate gasoline, diesel oil and gas; In addition, the injection of second stage charging, having stoped light constituent overcracking is less molecule, and object product yield is increased.
Accompanying drawing explanation
Fig. 1 is residual hydrocracking of the present invention and catalytic cracking combinational processing method process flow diagram.
Embodiment
Below in conjunction with accompanying drawing, method provided by the present invention is further detailed, but does not thereby limit the invention.
Technical process of the present invention is described in detail as follows, and catalytic cracking unit adopts riser reactor.
Residual oil raw material 1, after boosting, be mixed into boiling bed hydrogenation treatment reactor 2 with recycle hydrogen 5, by contacting with hydrotreating catalyst, remove the impurity such as part metals in stock oil, sulphur, nitrogen, reduce the carbon residue of raw material simultaneously, meet the charging requirement of downstream catalytic cracking unit as far as possible.Hydrotreating reactor 2 exports reaction effluent 3 and enters high-pressure separator 4 and carry out gas-liquid separation, isolated gaseous stream carries out after the laggard recycle compressors 8 of processing such as depriving hydrogen sulphide boost being recycled to hydrotreating reactor 2 entrances, the new hydrogen supplementing also can be introduced after recycle compressor 8, isolated liquid phase stream enters fractionation plant 6 by pipeline 16 and carries out fractionation, obtains light constituent and heavy constituent; Catalytic cracking reaction is carried out in the bottom that isolated light constituent enters catalytic cracking riser 9 by pipeline 7 by first step opening for feed; Heavy constituent, is isolated wax oil (being included in recycle stock) and is returned to catalytic unit as second stage charging to catalytic cracking fractionating tower 15 by pipeline 18, and heavy oil (being included in slurry oil) enters coker processing; Catalytic cracking reaction effluent 10 enters the separation column 15 of catalytic unit, isolates gas 11, gasoline 12, diesel oil 13, recycle stock 14 and slurry oil 17; Wherein gas 11, gasoline 12, diesel oil 13 dischargers, recycle stock 14 enters riser reactor 9 by second stage opening for feed, carries out catalytic cracking reaction; Slurry oil 17 enters coker and processes.
The following examples will further illustrate method provided by the invention, but not thereby limiting the invention.Reaction is to carry out on small riser formula catalytic cracking unit and pilot scale boiling bed residual oil hydrotreater.In embodiment and comparative example, stock oil used is to subtract slag in sand, and its character is listed in table 1.The type of embodiment and catalyst for hydrotreatment of residual oil used in comparative example is identical with volume, the molybdenum-nickel catalyzator take aluminum oxide as carrier that the boiling bed hydrogenation catalyst that process of the test is used is microspheroidal, wherein in catalyzer containing MoO
3for 15wt%, be 4wt% containing NiO, the bulk density of catalyzer is 0.75g/cm
3, specific surface area is 240m
2/ g, granules of catalyst mean diameter is 0.6mm.In the present invention, wt% is prime number mark.
Embodiment is identical with catalytic cracking catalyst used in comparative example, and fresh dose consists of: 95wt%LBO-16 olefine lowering catalyst+5wt%LBO-A improves octane enhancing additive (LBO-16 and LBO-A are the catalytic cracking catalyst of Lanzhou Petrochemical Company Development and Production).
Comparative example
This comparative example adopts conventional boiling bed residual oil hydrogenation and catalystic cracking method, and residual oil carries out hydrogenation reaction at hydrotreater, and reaction product isolated obtains gas and hydrogenated oil.The hydrogenated oil of gained together enters catalytic cracking unit and carries out cracking reaction, and one way is passed through, and product is gasoline, diesel oil, gas, and the above cut of catalytic cracking recycle oil loops back residual hydrogenation equipment and processes.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Embodiment
This embodiment adopts boiling bed residual oil hydrotreatment provided by the invention and catalytic cracking combination method, flow process is shown in Fig. 1, wherein hydrotreatment liquid product fractionates out light constituent and heavy constituent, its cut point is 350 ℃, second stage opening for feed is above first step charging, and distance the first opening for feed height accounts for 1/10 of riser tube height overall.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Comparing result shows, it is light constituent and heavy constituent that residual hydrogenation is generated to oil content, enter riser reactor from two-stage opening for feed respectively and carry out catalytic cracking reaction, compared with together entering catalyst cracker with the full cut of residual hydrogenation generation oil, liquefied gas, gasoline, diesel oil total recovery are 83.9wt%, exceed 17.5 percentage points than comparative example.Coke yield has declined 2.7 percentage points, and dry gas yied has declined 1.9 percentage points.The inventive method can meet the enterprise that wishes volume increase stop bracket gasoline well.
Table 1 stock oil character
Table 2 hydrotreatment and catalytic cracking process condition
Note: when * liquid, volume space velocity is for fresh residual oil raw material.
Table 3 product distributes
| Title | Comparative example | Embodiment | Difference |
| Catalytic cracking product distributes: wt% | |||
| Dry gas | 4.6 | 2.7 | -1.9 |
| Liquefied gas | 9.5 | 12.1 | +2.6 |
| Gasoline | 36.2 | 46.2 | +10.0 |
| Diesel oil | 18.3 | 23.2 | +4.9 |
| Slurry oil | 22.2 | 9.3 | -12.9 |
| Coke | 9.2 | 6.5 | -2.7 |
| Add up to | 100.0 | 100.0 | |
| Liquefied gas+gasoline+diesel oil, wt% | 64.0 | 81.5 | 17.5 |
Note: to install inlet amount as 100% calculating.
Table 4 catalytically cracked gasoline main products character
| Product | Comparative example | Embodiment |
| Density (20 ℃), g/cm 3 | 0.7402 | 0.7421 |
| S，μg/g | 38.6 | 30.2 |
| RON | 91.8 | 93.1 |
Claims (8)
1. a residual hydrocracking and catalytic cracking combination process, wherein catalytic cracking adopts riser reactor, described riser reactor arranges two-stage opening for feed, wherein first step opening for feed is arranged on the bottom of riser tube, second stage opening for feed is above first step opening for feed, and residual hydrocracking adopts boiling bed residual oil hydroprocessing technique, the method comprises: residual oil raw material enters boiling bed hydrogenation treatment reactor, under hydrogen and hydrotreating catalyst existence, carry out hydrogenation reaction, hydrogenation reaction effluent gas-liquid separation, liquid phase fractionates out light constituent and heavy constituent, and wherein the cut point of light constituent and heavy constituent is 320～380 ℃, as the catalytic cracking riser reactor first step, charging enters reactor by first step opening for feed to light constituent, heavy constituent enters separation column by the bottom of catalytic cracking fractionating tower, the entry position that heavy constituent enters catalytic cracking fractionating tower catalytic cracking reaction effluent enter catalytic cracking fractionating tower entry position above, heavy constituent and catalytic cracking reaction effluent are through fractionation, isolate dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil, wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage, enter reactor by second stage opening for feed, carry out catalytic cracking reaction,
In described riser reactor, second stage opening for feed is arranged on the top of first step opening for feed, accounts for 1/30～1/5 of whole riser tube height apart from the distance of first step opening for feed; The operational condition of boiling bed hydrogenation processing is: reaction pressure 6～30MPa, 400～490 ℃ of temperature of reaction, volume space velocity 0.1～5.0h when liquid
-1, hydrogen to oil volume ratio 200～2000; Catalytic cracking unit operational condition is: temperature of reaction is 480～550 ℃, and regeneration temperature is 600～800 ℃, and agent weight of oil ratio is 2～30, with 0.1～15.0 second duration of contact of catalyzer, and pressure 0.1～0.5MPa.
2. in accordance with the method for claim 1, it is characterized in that described slurry oil is as delayed coking feed component.
3. in accordance with the method for claim 1, it is characterized in that, riser tube second stage opening for feed is arranged on the top of first step opening for feed, accounts for 1/10～1/6 of whole riser tube height apart from the distance of first step opening for feed.
4. in accordance with the method for claim 1, it is characterized in that described residual oil raw material is long residuum or vacuum residuum.
5. in accordance with the method for claim 4, it is characterized in that, in residual oil raw material, also contain one or several in wax tailings, deasphalted oil, heavy distillate.
6. in accordance with the method for claim 4, it is characterized in that, the boiling bed hydrogenation catalyst that described boiling bed residual oil hydroprocessing technique adopts, carrier is one or more compositions in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or titanium oxide, take the weight of catalyzer as benchmark, nickel oxide or cobalt oxide are 1%～20%, and molybdenum oxide or Tungsten oxide 99.999 are 1%～30%; Catalyst property is as follows: bulk density is 0.4～0.9g/cm
3, particle diameter is 0.08～1.2mm, specific surface area is 100～300m
2/ g.
7. according to the method described in claim 1 or 6, it is characterized in that, the operational condition of boiling bed hydrogenation processing is: reaction pressure 15～20MPa, 420～470 ℃ of temperature of reaction, volume space velocity 0.5～2.0h when liquid
-1; Hydrogen to oil volume ratio 400～1000.
8. in accordance with the method for claim 1, it is characterized in that, catalytic cracking unit operational condition is: temperature of reaction is 480～550 ℃, regeneration temperature is 650～750 ℃, agent weight of oil ratio is 4～10, with catalyzer duration of contact be 0.5～5.0 second, pressure 0.1～0.5MPa.
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| CN103805256B (en) * | 2012-11-07 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of catalytic diesel oil reactive distillation process |
| CN104611049B (en) * | 2013-11-05 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of catalytic diesel oil reactive distillation process |
| CN103982739B (en) * | 2014-04-11 | 2016-08-17 | 中国石油化工股份有限公司青岛安全工程研究院 | The pre-thermal flow process of high temperature oil pulp grinder pump |
| CN108102710B (en) * | 2016-11-25 | 2019-10-15 | 中国石油化工股份有限公司 | A method of preparing needle coke |
| CN108102711B (en) * | 2016-11-25 | 2020-03-17 | 中国石油化工股份有限公司 | Combined process for producing needle coke |
| CN106833741A (en) * | 2017-02-08 | 2017-06-13 | 上海河图工程股份有限公司 | Boiling bed hydrogenation and RFCC combined method and hydrogenation catalyst |
| CN110055099B (en) * | 2019-05-21 | 2021-03-12 | 山东京博石油化工有限公司 | Treatment method of catalytic cracking recycle oil |
| CN114045179B (en) * | 2021-11-30 | 2023-04-11 | 陕西延长石油（集团）有限责任公司 | Multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system |
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| CN1896192A (en) * | 2005-07-15 | 2007-01-17 | 中国石油化工股份有限公司 | Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking |
| CN101463274A (en) * | 2007-12-20 | 2009-06-24 | 中国石油化工股份有限公司 | Improved hydrocarbon oil hydrotreating and catalytic cracking combined technique |
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| CN1896192A (en) * | 2005-07-15 | 2007-01-17 | 中国石油化工股份有限公司 | Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking |
| CN101463274A (en) * | 2007-12-20 | 2009-06-24 | 中国石油化工股份有限公司 | Improved hydrocarbon oil hydrotreating and catalytic cracking combined technique |
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