CN102311801A - Residual oil hydrogenation treatment and catalytic cracking combined method - Google Patents
Residual oil hydrogenation treatment and catalytic cracking combined method Download PDFInfo
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Abstract
The invention discloses a residual oil hydrogenation treatment and catalytic cracking combined method, which comprises the following components: performing the hydrogenation treatment reaction of a residual oil raw material in the presence of hydrogen and a hydrogenation catalyst, separating product of the reaction to obtain a gas, hydrogenated naphtha, hydrogenated diesel and hydrogenated tail oil, wherein the gas is circularly used in a hydrogenation reaction, the hydrogenated naphtha and hydrogenated tail oil enter a catalytic cracking device to undergo a catalytic cracking reaction in the presence of a cracking catalyst; and separating the product of the reaction to obtain a dry gas, a liquefied gas, a gasoline fraction and a catalytic cracking heavy fraction, wherein the catalytic cracking heavy fraction is filtered to remove solid impurity and circulated to a hydrogenation treatment device. When the method is used, the quality of produced naphtha and diesel product can be improved; and particularly, the sulfur content in naphtha and diesel is lowered and the cetane number of diesel is improved.
Description
Technical field
The present invention relates to a kind of residual oil lightening method, specifically with residual hydrocracking and catalytic cracking organic assembling, is the mainly process method of production premium and diesel product of raw material with residual oil.
Background technology
Along with crude oil becomes heavy day by day, becomes bad, increasing residual oil needs processing treatment.Processing treatment heavy, residual oil will be not lower boiling product with its cracking still, like petroleum naphtha, intermediate oil and vacuum gas oil etc., but also will improve their hydrogen-carbon ratio, and this just need realize through the method for decarburization or hydrogenation.Wherein decarbonization process comprises coking, solvent deasphalting, RFCC etc.; Hydrogenation comprises hydrogen cracking, unifining etc.Hydrogenation method can hydrocracking residual oil, improves the productive rate of liquid product, and can also remove heteroatoms wherein, and quality product is not bad.But hydrogenation method is the catalysis complete processing, has hydrogenation catalyst inactivation problem, and when especially processing poor quality, heavier hydrocarbon feeds, the catalyst deactivation problem is more serious.At present, in order to reduce heavy, poor residuum cost of processing, increase the oil refining enterprise profit; The technology of processing heavy, poor residuum is main with decarbonization process still, but its poor product quality need be carried out aftertreatment and could be utilized; Wherein deasphalted oil and wax tailings cut especially need carry out hydrotreatment; Could continue to use lighting devices such as catalytic cracking or hydrogen cracking to process, therefore, each oil refining enterprise all has the hydrotreater of deasphalted oil and wax tailings in addition.
The slag oil cracking rate of residual hydrocracking technology is lower, and main purpose is to supply raw materials for downstream raw material lighting device such as devices such as catalytic cracking or coking.Through hydrotreatment; Sulphur, nitrogen, metal impurities content and carbon residue in the poor residuum are obviously reduced; Thereby obtain the charging that lighting device in downstream can be accepted; Especially be mainstream technology with residue fixed-bed hydrotreatment and catalytic cracking combination technique in the CCU, therefore heavy at present, residual hydrogenation modifying process technology.
Existing residual hydrocracking and catalytic cracking combined technique; At first be that residual oil is carried out hydrotreatment; Hydrogenated oil is isolated petroleum naphtha and diesel oil distillate; Hydrogenation tail oil carries out catalytic cracking reaction as the RFCC charging, and product is dry gas, liquefied gas, gasoline, diesel oil and coke; Recycle stock carry out the catalysis freshening or with loop back residual hydrogenation equipment and the residual hydrocracking raw materials mix is carried out hydrotreatment, catalytic slurry gets rid of outward or part catalysis freshening or loop back residual hydrogenation equipment.Above-mentioned residual hydrocracking and catalytic cracking combined technique exist yield of gasoline low, and heat energy loss is big, unfavorable factors such as facility investment height.
US4,713,221 disclose on the residual hydrogenation of routine and catalytic cracking combined basis, and the heavy cycle oil of catalytic cracking is circulated to residual hydrogenation equipment, and carry out hydrogenation after residual oil mixes, and get into CCU again.But catalytically cracked oil is not utilized effectively, and this method is limited to reduction coke yield, raising product yield.
CN1119397C discloses a kind of hydrogenation and catalystic cracking combined process for residual oil; In this method; Residual oil and clarified oil get into residual hydrogenation equipment together, in the presence of hydrogen and hydrogenation catalyst, react, and heavy cycle oil circulates in CCU inside; The slurry oil of reaction gained obtains clarified oil through separator separates, is back to hydrogenation unit.But slurry oil gets into the residual hydrocracking device, and the easy green coke thing in the slurry oil will increase the carbon deposit of hydrogenation catalyst, has reduced the hydrogenation activity and the operational cycle of hydrogenation catalyst, and heavy cycle oil is inner at CCU.Therefore, this method is limited to reducing coke yield, improving the quality of products.
CN1382776A discloses the method for a kind of residual hydrocracking and catalytically cracking heavy oil, and this method is carried out hydrogenation reaction with residual oil at hydrotreater, and reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue.The hydrogenated residue of gained gets into CCU with optional vacuum gas oil and carries out cracking reaction, and the heavy cycle oil of catalytic cracking returns hydrotreater, and the thing that steams that the distillation slurry oil obtains returns hydrotreater.This method is organically joined together two devices, can residual oil, heavy cycle oil and slurry oil be converted into clean cargo.But this method all is provided with fractionating system in hydrotreatment and catalytic cracking process, increased investment cost; Because the process heat exchange, heat-energy losses is more; Simultaneously, hydrotreater and CCU all have diesel product, and comparatively speaking, the total recovery of gasoline and gas products will reduce.In addition, the slag oil cracking rate of residual hydrocracking device is lower, and it is limited that hydrogenated oil carries out petroleum naphtha, diesel yield that fractionation obtains.Foreign matter contents such as catalytic cracking diesel oil sulphur are higher, and character is relatively poor, also need further hydrotreatment just to can be used as qualified diesel product.
In residual hydrocracking and the catalytic cracking combined technique, how improving hydrotreated naphtha and catalytic cracking diesel oil quality, also is the content that needs emphasis to consider.
Summary of the invention
To the deficiency of prior art, the present invention provides a kind of residual hydrocracking and catalytic cracking combination method, can improve and produce petroleum naphtha and diesel product quality, particularly reduced petroleum naphtha and diesel oil sulphur content, improved diesel cetane-number.
Residual hydrocracking of the present invention and catalytic cracking combination method comprise: residual oil raw material carries out the hydrotreatment reaction in the presence of hydrogen and hydrogenation catalyst; Reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil; Gas circulation is used for hydrogenation reaction; Hydrotreated naphtha and oxygenation tail oil get into CCU; In the presence of cracking catalyst, carry out catalytic cracking reaction, reaction product isolated obtains dry gas, liquefied gas, gasoline fraction and catalytic cracking last running, and catalytic cracking last running is circulated to hydrotreater after filtering out solid impurity.
In the inventive method, residual oil raw material comprises long residuum or vacuum residuum, can be the residual oil raw material in other source also, also can contain simultaneously in the residual oil raw material among a kind of or several in part wax tailings, deasphalted oil, the heavy distillate.
The residual hydrogenation technology can be any technology of the present invention that is applicable to, like fixed bed residual hydrocracking technology, suspension bed residual oil hydrogenation treatment technology, boiling bed residual oil hydrotreatment technology, moving-bed residual hydrocracking technology etc.With more sophisticated fixed bed residual hydrocracking technology in the present industry is example, the catalyst for hydrotreatment of residual oil of employing be meant have residuum hydrogenating and metal-eliminating, the single catalyst or the combination catalyst of function such as hydrogenating desulfurization, hydrodenitrification and hydrogen cracking.These catalyzer generally all are to be carrier with porous refractory inorganic oxides such as aluminum oxide; The oxide compound of group vib and/or VIII family metal such as W, Mo, Co, Ni etc. is an active ingredient; The catalyzer that optionally adds elements such as other various auxiliary agents such as P, Si, F, B; The CEN that is for example produced by catalyzer branch office of Sinopec Group, FZC, ZTN, ZTS series residual oil hydrocatalyst, ZTN, the ZTS catalyst series produced by first fertilizer plant of Qilu Petrochemical company just belong to this type catalyzer.At present in fixed bed residual hydrogenation technology; It often is the supporting use of multiple catalyzer; Protective material, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst are wherein arranged, and the filling order generally is that raw oil is contacted with protective material, HDM, hydrogenating desulfurization, hydrodenitrogenation catalyst successively.Technology with these several kinds of catalyst mix fillings is also arranged certainly.The a plurality of reactor drums of hydrotreatment operated by rotary motion are to improve amount of finish.Be 5MPa-35MPa in absolute pressure normally, preferably 10MPa-20MPa, temperature of reaction are 300 ℃-500 ℃, preferably 350 ℃-450 ℃ operations down.Volume space velocity and hydrogen dividing potential drop are to select according to the characteristic of treating material and the transformation efficiency and the refining depth of requirement during liquid.Volume space velocity is generally at 0.1h during fresh residual oil raw material liquid
-1-5.0h
-1, 0.15h preferably
-1-2.0h
-1Scope in, total hydrogen to oil volume ratio is 100-5000, is preferably 300-3000.The present invention is applicable to normal pressure and vacuum residuum hydrotreatment, is particularly useful for the hydrocracking of heavy hydrocarbon oil.The actual conditions of residual hydrocracking process can specifically be confirmed according to the requirement of raw material properties and CCU charging.
In the inventive method, catalytic cracking can be adopted this area routine techniques.CCU can be that every covering device should comprise a reactor drum, a revivifier at least more than a cover or overlapped.CCU is provided with separation column, can set respectively by every cover CCU, also can be shared.Catalytic cracking fractionating tower is dry gas, liquefied gas, catalytically cracked gasoline and catalytic cracking last running with the fractionation of catalytic cracking reaction elute.Catalytic cracking fractionating tower is compared with conventional catalytic cracking fractionating tower can simplified design, only fractionates out dry gas, liquefied gas and catalytically cracked gasoline, and catalytic cracking last running comprises catalytic cracking diesel oil, heavy catalytic cycle oil and slurry oil.Catalytic cracking last running filters out the micro-catalytic cracking catalyst powder that contains earlier before looping back hydrotreater.
CCU is operated by this area general condition: temperature of reaction is 450～600 ℃, preferably 480～550 ℃; Regeneration temperature is 600-800 ℃, is preferably 650-750 ℃, and the agent weight of oil is than 2～30, preferably 4～10; With 0.1～15 second duration of contact of catalyzer, best 0.5～5 second; Pressure 0.1～0.5MPa.The catalytic cracking catalyst that is adopted comprises the catalyzer that is generally used for catalytic cracking; Like silica-alumina catalyst, silica-magnesia catalyst, acid-treated carclazyte and X type, Y type, ZSM-5, M type, layer post equimolecular sieve cracking catalyst; Molecular sieve cracking catalyst preferably, this is because molecular sieve cracking catalyst active high, green coke is few; Gasoline yield is high, and transformation efficiency is high.The reactor drum of described CCU can be the catalyst cracker of various types, and preferably riser reactor or riser tube add the bed reactor drum.Technical process is generally: raw oil injects from the riser reactor bottom; Contact with 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, accomplish the catalytic cracking reaction of whole raw oil.
The concrete operations condition of residual hydrocracking and catalytic cracking can be obtained through simple experiment according to feedstock property and product quality indicator by the technician.
The invention has the advantages that:
1, in whole combination process, main products is high hexadecane value low sulfur content hydrogenated diesel oil, high-octane rating low sulfur content catalytically cracked gasoline, LPG liquefied petroleum gas and a small amount of dry gas.The fractionating system of catalytic cracking reaction elute is not carried out the catalytic cracking diesel oil fraction separation among the present invention, saves the repetition procedure of processing.Simultaneously, the catalytic cracking fractionating system can be simplified greatly, reduces facility investment and operation energy consumption.
2, the catalytic cracking reaction elute is not isolated catalytically cracked oil, has solved slurry oil goes out catalyst solid powder because of viscosity is very much not easily separated problem.Contain diesel oil distillate in the catalytic cracking heavy distillate, because the diluting effect of diesel oil distillate, the cycle oil slurry viscosity significantly reduces, and makes catalyst solid powder filtration wherein be more prone to.When conventional catalytically cracked oil separated, though can part utilize through clarification, utilization ratio was lower, and the inventive method does not produce and effluxes part owing to do not isolate catalytically cracked oil, has improved the yield of utilization ratio of raw materials and purpose product.
3, from whole combination process, select hydrotreated naphtha to get into catalyst cracker in the hydrotreater with hydrogenation heavy oil, avoided generating second-rate hydrotreated naphtha; And be converted into quality catalytic cracking petroleum naphtha preferably; Octane value can be improved, and simultaneously, catalytically cracked material is also played diluting effect; Reduced the viscosity of raw material, the conveying and the filtration of mixing raw material oil are more prone to.
4, from whole combination process; Catalytic cracking diesel oil cut and above last running directly together slag input oil hydrogenation technique process remove impurity, aromatic hydrocarbons is saturated, has avoided generating second-rate catalytic cracking diesel oil; And changing quality hydrogenated diesel oil preferably into, cetane value is significantly improved.
5, catalytic cracking last running is played diluting effect to fresh residual oil raw material, and oil property improves, and has reduced the hydrogenation reaction difficulty and processing severity of residual hydrocracking parallel feeding; In addition; Catalytic cracking last running can reduce the viscosity of raw material, improves logistics distribution and the mass transfer of raw material in reactive system, reduces to be diffused in the influence in the residual hydrocracking process; Improve the deposition distribution of poisonous metal in catalytic reaction system such as nickel, vanadium, prolong the work-ing life of catalyzer; Simultaneously, the reduction of viscosity is more prone to the conveying and the filtration of mixing raw material oil.
Description of drawings
Fig. 1 is residual hydrocracking of the present invention and catalytic cracking combination method process flow diagram.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further explained, but therefore do not limited the present invention.
Technical process is described in detail as follows:
Catalytic cracking last running 15 after residual oil raw material 2 and the filtration mixes; Be mixed into hydrotreating reactor 3 with recycle hydrogen 1 after boosting; Through contacting with the hydrotreating catalyst bed; Remove impurity such as metal in the raw oil, sulphur, nitrogen, the carbon residue that reduces raw material simultaneously satisfies the charging requirement of downstream catalytic cracking unit.The reaction product of separating residual hydrogenation; Obtain gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue; Wherein gas and hydrogenated diesel oil be respectively through pipeline 4,6 caterpillars, and hydrotreated naphtha 5 and hydrogenated residue 7 get into the reactive system 9 of CCU together through pipeline 8, contacts with the high temperature regeneration catalytic cracking catalyst and react; Catalytic cracking gas that obtains and catalytic cracking petroleum naphtha are respectively through pipeline 10,11 dischargers; Remainingly get into separators 13 as catalytic cracking last running 12, filter out catalyst fines, mechanical impurity and solid particulate 14, the catalytic cracking last running 15 after the filtration is recycled to hydrotreater 3.
Following embodiment will further specify method provided by the invention, but therefore not limit the present invention.Reaction is on small-sized lifting tubular type CCU and pilot scale residual hydrocracking device, to carry out.Used raw oil is normal slag in the sand in embodiment and the Comparative Examples, and its character is listed in table 1.The type of used catalyst for hydrotreatment of residual oil and volume are identical in embodiment and the Comparative Examples; All are CEN, FZC, ZTN, ZTS series residual oil hydrocatalysts that catalyzer branch office of Sinopec Group produces; Specifically comprise protective material; Catalyst for demetalation, desulfurization catalyst, denitrification catalyst etc.; The filling order generally is that raw oil is contacted with protective material, HDM, hydrogenating desulfurization, hydrodenitrogenation catalyst successively, and the technology with these several kinds of catalyst mix fillings is also arranged certainly.The technology contents that above-mentioned catalyst loading technology is well known to those skilled in the art.Catalytic cracking catalyst used in embodiment and the Comparative Examples is identical, is the catalyzer that 3,500,000 tons of/year heavy oil catalytically cracking equipments of Dalian Company use, and is industrial equilibrium catalyst.
Its fresh dose consists of: 95wt%LBO-16 olefine lowering catalyst+5wt%LBO-A boosting of octane rating auxiliary agent.
Comparative Examples
This Comparative Examples adopts conventional residual hydrocracking-catalyst cracking method, and promptly residual oil carries out hydrogenation reaction at hydrotreater, and reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue.The hydrogenated residue of gained gets into CCU and carries out cracking reaction, and heavy catalytic cycle oil is handled at the CCU internal recycle.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Embodiment
This embodiment adopts residual hydrocracking provided by the invention and catalytic cracking combination method; Hydrotreatment gained liquid product fractionates out hydrotreated naphtha, diesel oil and hydrogenation tail oil; Hydrotreated naphtha and hydrogenation tail oil advance CCU together; Catalytic cracking reaction elute fractionating system simplified design; Only fractionate out dry gas, liquefied gas and gasoline fraction, catalytic cracking diesel oil, catalytic cycle oil and catalytic slurry do not carry out fractionation directly as catalytic cracking last running, and catalytic cracking last running is circulated to further processing in the hydrotreater after filtering out solid impurity.Table 2, table 3, table 5 are respectively processing condition, product distributes and main products character.
Comparing result shows; The inventive method is when main products yields such as guaranteeing gasoline fraction, diesel oil distillate slightly improves; Obviously improved the quality of gasoline and diesel product; The sulphur content of gasoline and diesel product is reduced to 29.5 μ g/g, 90.1 μ g/g by 55.2 μ g/g, 3055 μ g/g respectively, and diesel-fuel cetane number brings up to 47 by 21.5.The inventive method can satisfy the requirement of enterprise production high quality gasoline and diesel well.
Table 1 raw oil character
| Project | Data |
| S, quality % | 2.33 |
| N，μg/g | 3044 |
| Carbon residue (CCR), quality % | 11.8 |
| Density (20 ℃), kg/m 3 | 982.0 |
| Viscosity (100 ℃), mm 2/s | 98.0 |
| Ni+V，μg/g | 75.62 |
Table 2 hydrotreatment and catalytic cracking process condition
| Title | Comparative Examples | Embodiment |
| The hydroprocessing technique condition | ||
| Raw material | Fresh feed | Fresh feed+catalytic cracking last running |
| The hydrogen dividing potential drop, MPa | 14.0 | 14.0 |
| Temperature of reaction, ℃ | 385 | 385 |
| Volume space velocity, h -1 | 0.20 | 0.27 |
| Hydrogen-oil ratio | 600 | 600 |
| The catalytic cracking process condition | ||
| Raw material | The normal slag of hydrogenation | The mixing oil hydrogenated oil |
| Temperature of reaction, ℃ | 505 | 505 |
| Agent-oil ratio | 7.5 | 7.5 |
● calculate with the device inlet amount.The inlet amount of fresh feed is identical with Comparative Examples among the embodiment.
Table 3 product distributes
| Title | Comparative Examples | Embodiment |
| The hydrotreatment product distributes: quality % | ||
| Chemistry hydrogen consumption | 1.20 | 1.53 |
| Gas | 2.54 | 2.66 |
| Petroleum naphtha | 1.14 | - |
| Diesel oil | 5.25 | 28.30 |
| Hydrogenation tail oil | 92.27 | 70.57 |
| The catalytic cracking product distributes: quality % | ||
| Dry gas | 1.91 | 2.12 |
| Liquefied gas | 15.54 | 16.52 |
| Gasoline | 46.94 | 49.50 |
| Diesel oil | 19.40 | - |
| Slurry oil | 7.47 | - |
| Coke | 8.74 | 7.12 |
● with single covering device inlet amount is 100% calculating.
The conventional wax oil hydrogenation processing-catalytic cracking of table 4 main products character
● the normal slag of hydrogenation, heavy catalytic cycle oil are intermediates in the present invention
Table 5 main products character of the present invention
| Product | Catalytically cracked gasoline | Hydrogenated diesel oil |
| Density (20 ℃), g/cm 3 | 0.74 | 0.9134 |
| S，μg/g | 29.5 | 90.1 |
| Octane value/cetane value | 91.9 | 47 |
Claims (10)
1. residual hydrocracking and catalytic cracking combination method; It is characterized in that: residual oil raw material carries out the hydrotreatment reaction in the presence of hydrogen and hydrogenation catalyst; Reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil; Gas circulation is used for hydrogenation reaction, and hydrotreated naphtha and hydrogenation tail oil get into CCU, in the presence of cracking catalyst, carry out catalytic cracking reaction; Reaction product isolated obtains dry gas, liquefied gas, gasoline fraction and catalytic cracking last running, and catalytic cracking last running is circulated to hydrotreater after filtering out solid impurity.
2. according to the described method of claim 1, it is characterized in that: residual oil raw material comprises long residuum or vacuum residuum.
3. according to the described method of claim 1, it is characterized in that: the residual oil raw material hydrogenation adopts fixed bed residual hydrocracking technology, suspension bed residual oil hydrogenation treatment technology, boiling bed residual oil hydrotreatment technology or moving-bed residual hydrocracking technology.
4. according to claim 1 or 3 described methods, it is characterized in that: residual oil raw material hydrogenation process condition is: absolute pressure is 5MPa-35MPa, and temperature is 300 ℃-500 ℃, and volume space velocity is 0.1h during fresh liquid
-1-5.0h
-1, total hydrogen to oil volume ratio is 100-5000.
5. according to claim 1 or 3 described methods, it is characterized in that: residual oil raw material hydrogenation process condition is: absolute pressure is 10MPa-20MPa, and temperature is that volume space velocity is 0.15h during fresh liquid under 350 ℃-450 ℃
-1-2.0h
-1, total hydrogen to oil volume ratio is 300-3000.
6. according to the described method of claim 1, it is characterized in that: CCU is that every cover CCU should comprise a reactor drum and a revivifier at least more than a cover or overlapped.
7. according to the described method of claim 6, it is characterized in that: CCU is provided with separation column, and catalytic cracking fractionating tower is dry gas, liquefied gas, catalytically cracked gasoline and catalytic cracking last running with the fractionation of catalytic cracking reaction elute.
8. according to claim 1 or 7 described methods, it is characterized in that: catalytic cracking last running filters out the micro-catalytic cracking catalyst powder that contains earlier before looping back hydrotreater.
9. according to claim 1 or 6 described methods; It is characterized in that: the CCU operational condition is: temperature of reaction is 450-600 ℃, and regeneration temperature is 600-800 ℃, and the agent weight of oil compares 2-30; With catalyzer 0.1-15 duration of contact second, pressure 0.1-0.5MPa.
10. according to the described method of claim 1, it is characterized in that: the CCU operational condition is: temperature of reaction is 490-550 ℃, and regeneration temperature is 650-750 ℃, and the agent weight of oil is than 4-10, with catalyzer 0.5-5 duration of contact second.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106957680A (en) * | 2015-12-23 | 2017-07-18 | 阿克森斯公司 | The apparatus and method of the sour gas of common compression hydro-conversion or hydrotreating unit and the gaseous effluent of catalytic cracking unit |
| CN107779226A (en) * | 2016-08-29 | 2018-03-09 | 中国石油化工股份有限公司 | The method of low-carbon olefines high-output and the system for low-carbon olefines high-output |
| CN114075454A (en) * | 2020-08-20 | 2022-02-22 | 中国石油化工股份有限公司 | Oil slurry and heavy oil processing system and method |
| CN114075455A (en) * | 2020-08-20 | 2022-02-22 | 中国石油化工股份有限公司 | Catalytic cracking and residual oil hydrogenation combined treatment system and method |
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| 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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| US4713221A (en) * | 1984-05-25 | 1987-12-15 | Phillips Petroleum Company | Crude oil refining apparatus |
| CN1382776A (en) * | 2001-04-28 | 2002-12-04 | 中国石油化工股份有限公司 | Process for hydrogenating residual oil and catalytically cracking heavy oil |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106957680A (en) * | 2015-12-23 | 2017-07-18 | 阿克森斯公司 | The apparatus and method of the sour gas of common compression hydro-conversion or hydrotreating unit and the gaseous effluent of catalytic cracking unit |
| CN106957680B (en) * | 2015-12-23 | 2020-07-24 | 阿克森斯公司 | Apparatus and method for co-compressing acid gas of a hydroconversion or hydrotreatment unit and gas effluent of a catalytic cracking unit |
| CN107779226A (en) * | 2016-08-29 | 2018-03-09 | 中国石油化工股份有限公司 | The method of low-carbon olefines high-output and the system for low-carbon olefines high-output |
| CN107779226B (en) * | 2016-08-29 | 2020-01-10 | 中国石油化工股份有限公司 | Method for producing more low-carbon olefins and system for producing more low-carbon olefins |
| CN114075454A (en) * | 2020-08-20 | 2022-02-22 | 中国石油化工股份有限公司 | Oil slurry and heavy oil processing system and method |
| CN114075455A (en) * | 2020-08-20 | 2022-02-22 | 中国石油化工股份有限公司 | Catalytic cracking and residual oil hydrogenation combined treatment system and method |
| CN114075455B (en) * | 2020-08-20 | 2023-06-09 | 中国石油化工股份有限公司 | Catalytic cracking and residual oil hydrogenation combined treatment system and method |
| CN114075454B (en) * | 2020-08-20 | 2023-06-09 | 中国石油化工股份有限公司 | Slurry oil and heavy oil processing system and method |
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