CN104560186B - Catalytic conversion method capable of realizing maximum gasoline production - Google Patents
Catalytic conversion method capable of realizing maximum gasoline production Download PDFInfo
- Publication number
- CN104560186B CN104560186B CN201310517650.9A CN201310517650A CN104560186B CN 104560186 B CN104560186 B CN 104560186B CN 201310517650 A CN201310517650 A CN 201310517650A CN 104560186 B CN104560186 B CN 104560186B
- Authority
- CN
- China
- Prior art keywords
- catalytic cracking
- oil
- reaction
- light cycle
- cycle oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a catalytic conversion method capable of realizing maximum gasoline production. Catalytic cracking light cycle oil is cut to obtain a light fraction and a heavy fraction, wherein the heavy fraction is hydrotreated to obtain a hydrogenated heavy fraction; the light fraction and the hydrogenated heavy fraction are independently layered by use of different nozzles to go into a catalytic cracking device to have a cracking reaction in the presence of a catalytic cracking catalyst; and the reaction product is separated to obtain a product comprising gasoline and light cycle oil. According to the catalytic conversion method, the independent catalytic cracking device is adopted to process the light fraction and the hydrogenated heavy fraction of the light cycle oil and feed the fractions layer by layer; as a result, the harsh conditions needed by the catalytic cracking reactions of different fractions of the light cycle oil can be optimized and satisfied to the utmost extent, and the catalytic gasoline can be produced to the utmost extent.
Description
Technical field
The invention belongs to the catalysis conversion method of petroleum hydrocarbon in the absence of hydrogen, more specifically, is a kind of
The catalysis conversion method of the gasoline of production is maximized by catalytic cracking light cycle oil.
Background technology
With the development of crude oil heaviness and rapid growth of the market to light-end products demand, in China, as heavy oil lightweight
The catalytic cracking technology of change is rapidly developed.However, it is necessary to the fact for facing is catalytic cracking diesel oil（Or claim " gently to follow
Ring oil "）Quality it is but relatively poor always, density is big, and arene content is high, and Cetane number is low, even if passing through diesel oil hydrogenation modification
Technology is also difficult to reach increasingly strict diesel oil regulation.How to solve catalytic cracking light cycle oil and be one increasingly serious to ask
Topic.Simultaneous another question is domestic gasoline product chronic shortage, and catalytically cracked gasoline accounts for gasoline product
80%.Therefore, how not produce and gently follow realizing heavy charge to maximize production high-knock rating gasoline by catalytic cracking process
Ring oil is probably the new way for solving the above problems.
US4585545 discloses one kind and catalytic cracking light cycle oil full fraction is first carried out hydrotreating, the hydrogenation for obtaining
Diesel oil removes catalytic cracking catalysis conversion method of the production rich in mononuclear aromatics gasoline again.
The method that CN1422327A discloses a kind of modification of catalytic cracking light cycle oil, is by the with mink cell focus as raw material
The light cycle oil of one catalytic cracking unit production carries out deep hydrogenation, and the hydrogenation recycle oil for obtaining enters the second catalytic cracking dress again
Put.On the basis of the method, CN1423689A emphasizes catalyst requirement the selecting containing 50-95% in the second catalytic cracking unit
Large pore zeolite of the aperture of shape zeolite and about 5-50% greater than or equal to about 0.7nm, optionally to improve light olefins yields.
CN1466619A discloses a kind of method for transformation of catalytic cracking light cycle oil, is to react catalytic cracking riser
Device is divided into upstream and downstream two reaction zones, wherein mink cell focus injection catchment, its hydrogenated place of catalytic cracking production light cycle oil
The hydrogenation recycle oil injection upstream obtained after reason.On the basis of the method, the charging in CN1425054A method middle and lower reaches area
In addition to being hydrogenated with recycle oil, Petroleum is also add.In the method, not only hydrogen consumption is high, and is hydrogenated with recycle oil in upstream reaction
The conversion of the mink cell focus in downstream can be had a strong impact on.
From document disclosed above it is found that one of important channel being processed for catalytic cracking light cycle oil is
Which is first carried out hydrotreating, then catalytic cracking again.It must be noted that light cycle oil is regardless of whether hydrogenation, and mink cell focus
Macromole is compared, and its molecule is little, bond energy big, therefore how to control the key that the operating parameter of catalytic cracking is light cycle oil processing
One of.If additionally, light cycle oil is hydrogenated with, the operational control of hydrogenation process is also one of key of light cycle oil processing.
The content of the invention
The purpose of the present invention is to provide a kind of catalysis conversion method for maximizing gasoline production on the basis of existing technology.
The catalysis conversion method that the present invention is provided includes：
（1）Catalytic cracking light cycle oil is cleaved to obtain light fraction and heavy distillat；
（2）Step（1）The heavy distillat carries out hydrotreating reaction in the presence of hydrogen and hydrotreating catalyst, separates
Product obtains being hydrogenated with heavy distillat；
（3）Step（1）The light fraction, step（2）Riser reactor is entered separately through different spray nozzles layering, is being urged
Catalytic cracking reaction is carried out in the presence of fluidized cracking catalysts, is separated catalytic cracking catalyst to be generated and reaction oil gas, is wherein reacted
Oil gas is isolated to the product including gasoline, light cycle oil.
It is preferred that the method also includes：Step（3）The catalytic cracking catalyst to be generated gained regeneration Jing after stripping, regeneration is urged
Fluidized cracking catalysts return riser reactor and recycle.
Step（1）The catalytic cracking light cycle oil is selected from the produced light cycle oil of allocatalysis cracking unit or/and we
Method catalytic cracking unit step（3）Produced light cycle oil, preferably the produced light cycle oil of allocatalysis cracking unit and this method are urged
Change cracking unit step（3）Produced light cycle oil.
The method that the present invention is provided is specific as follows：
Catalytic cracking light cycle oil is cut into single fractionating column, and cutting temperature is controlled at 250～260 DEG C, excellent
Cutting temperature is selected for 260 DEG C, the not higher than light fraction of the cutting temperature is respectively obtained from the top and bottom of fractionating column and is higher than
The heavy distillat of the cutting temperature.
Hydrotreater is removed in the heavy distillat, carries out hydrotreating reaction in the presence of hydrogen and hydrogenation catalyst, plus
Hydrogen treatment conditions are：10.0～25.0MPa of hydrogen dividing potential drop, preferably 10.0～22.0MPa；330～450 DEG C of reaction temperature, preferably 340
～380 DEG C；Volume space velocity 0.1～2.0 hour-1, 1000～2000Nm of hydrogen to oil volume ratio3/m3.Separate product and obtain fore-running
The fraction of 250 DEG C of point ＞, 260 DEG C of preferred ＞, or claim hydrogenated diesel oil, hydrogenation heavy distillat.In the hydrogenation heavy distillat, double ring arene contains
Amount wants≤10 heavy %, preferably≤8 heavy %.
Described activity of hydrocatalyst metal component is selected from vib metals and/or group VIII base metal, carrier
In aluminium oxide, silicon dioxide, amorphous silica-alumina any one or several.The vib metals are molybdenum or/and tungsten, the
VIII base metal is nickel or/and cobalt.The combination of the preferred nickel-tungsten of active metal component, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
The light fraction of light cycle oil and the hydrogenation heavy distillat for obtaining enter single catalytic cracking unit, urge in catalytic cracking
Cracking reaction is carried out in the presence of agent, is separated product and is obtained dry gas, liquefied gas, gasoline, light cycle oil, slurry oil, coke.Urge
The concrete operations condition for changing cracking unit is as follows：
Catalytic cracking unit can be isometrical riser reactor or reducing riser reactor.≤ 260 DEG C of light fraction
Enter riser reactor after can mixing with the hydrogenation heavy distillat for obtaining together, but preferably separate to enter separately through different spray nozzles
Enter riser reactor.Wherein underlying nozzle of the light fraction from riser（Upstream）Into, and heavy distillat is hydrogenated with from riser
Upper strata nozzle（Downstream）Into.The distance of upper and lower layer nozzle is controlling the time of staying of the reaction oil gas in two-layer nozzle distance
It was advisable for 0.01～3 second, preferably 0.05～1 second.The advantage that light fraction and hydrogenation heavy distillat layering are entered can be that optimization meets
The reaction condition of different fractions catalytic cracking, so that realize farthest converting.
The reaction condition of catalytic cracking unit is：Reaction temperature is 520～650 DEG C, preferably 550～590 DEG C；Agent oil quality
Than 5～100, preferably 8～50；The 1-10 seconds oil gas time of staying, preferably 2～8 seconds；Pressure（Absolute pressure）0.15～0.4MPa；
Water vapour is 0.01～0.5 preferably 0.02～0.2 with the weight ratio of raw material；Catalyst Balance Activity（MAT）>=65, preferably >=
68。
Catalytic cracking catalyst includes zeolite, inorganic oxide and optional clay.The content of each component is respectively：Zeolite
10～50 weight %, 5～90 weight % of inorganic oxide, 0～70 heavy % of clay.Wherein active component be selected from the Y with or without rare earth,
One kind in HY, USY or Beta zeolite, two or more.
It is an advantage of the current invention that：
1st, catalytic cracking unit light cycle oil is first cut, and wherein heavy distillat will removes hydrogenation, can be subtracted to greatest extent
Few hydrogen consumption；
2nd, using single catalytic cracking unit process light cycle oil light fraction and hydrogenation after heavy distillat and be layered into
Enter, the harsh conditions met needed for light cycle oil different fractions catalytic cracking reaction can be optimized to greatest extent, so as to maximum
Degree ground production catalytic gasoline.
Description of the drawings
The catalysis conversion method schematic flow sheet of the maximization gasoline production that Fig. 1 is provided for the present invention.
Specific embodiment
Method provided by the present invention is further illustrated below in conjunction with the accompanying drawings, but therefore the present invention is not subject to any limit
System.
The catalysis conversion method schematic flow sheet that accompanying drawing is provided for the present invention.
Fig. 1 is the schematic flow sheet of the preferred forms of the present invention, but does not limit the present invention.The shape of equipment and pipeline
Shape, size are not limited by the accompanying figures, but determine as the case may be.In accompanying drawing, each numbering is described as follows:
1st, 3-5,7,11-14 represent pipeline；2 is fractionating device；6 is diesel hydrotreating unit；8th, 9 is catalytic cracking feeds
Nozzle；10 is catalytic cracking reaction device.
Below in conjunction with the accompanying drawings preferred forms provided by the present invention are further described.
Catalytic cracking light cycle oil Jing pipelines 1 are cut into fractionating device 2, obtain≤260 DEG C of light fraction and ＞
260 DEG C of heavy distillat.Wherein≤260 DEG C of light fraction Jing pipelines 3, catalytic cracking lower floor feed nozzle 8 enter Catalytic Cracking Unit of Measure
Answer device 10.And the double distilled lease making pipeline 4 of 260 DEG C of ＞ enters diesel hydrotreating unit 6, hydrogen Jing pipelines 5 introduce diesel oil simultaneously and add
Hydrogen production device 6.Product hydrogenated diesel oil Jing pipelines 7, catalytic cracking upper strata nozzle 9 after hydrogenation enter catalytic cracking reaction device 10.
≤ 260 DEG C of light fraction and hydrogenated diesel oil in catalytic cracking unit 10 in the presence of catalytic cracking catalyst carry out catalysis and split
Change reaction, the high-knock rating gasoline Jing pipelines 11 that separation product is obtained are drawn, and another catalytic cracking reaction product is gently circulated
Oily Jing pipelines 12 are drawn, Jing pipelines 13,14,1 are circulated into fractionating device 2.For simplicity, other products such as dry gas, liquefaction
Gas, slurry oil etc. are not drawn in figure.
The following examples will be further described to the present invention, but not thereby limiting the invention.In embodiment
The hydrotreating catalyst commercial grades of filling are RN-32V in hydrotreating fixed bed reactors, and protective agent commercial grades are
RG-1, hydrotreating catalyst and protectant admission space ratio are 95：5, produced by Sinopec catalyst branch company.
In embodiment, comparative example catalytic cracking unit using the physico-chemical property of catalyst be shown in Table 1, its commercial grades is
HAC, is produced by Sinopec catalyst branch company.
Raw material used in embodiment, comparative example（Catalytic cracking light cycle oil）Property is listed in table 2.
Embodiment
This example demonstrates that using the present invention provide method, raw material elder generation Jing boiling ranges cutting obtain light cycle oil light fraction with
Light cycle oil heavy distillat, cut point are 250 DEG C.
Light cycle oil heavy distillat enters medium-sized hydrogenation plant, and the experimental condition of hydrogenation is：Hydrogen dividing potential drop 12.0MPa；Average bed
360 DEG C of reaction temperature of layer, volume space velocity 0.5 hour-1, hydrogen to oil volume ratio 1400Nm3/m3.In hydrogenation heavy distillat, double ring arene contains
Measure as 4.9 heavy %.
Light cycle oil heavy distillat after light cycle oil light fraction and hydrogenation respectively enters medium-sized catalytic cracking riser reaction
The upper and lower layer nozzle of device, wherein light fraction enter underlying nozzle, and upper strata nozzle is entered in hydrogenation heavy distillat.Upper and lower two-layer nozzle away from
It it is 0.5 second from the time of staying for being reaction oil gas in two-layer nozzle distance.The main operating parameters of kitty cracker
For：570 DEG C of reaction temperature；Agent oil quality compares 20；7 seconds oil gas time of staying；Pressure（Absolute pressure）0.25MPa；Water vapour with
The weight ratio of raw material is 0.06.The micro-activity of poising agent（MAT）For 68.
Comparative example 1
Medium-sized tester and catalyst are identical with embodiment.The same embodiment of boiling range cut point of light cycle oil, only
It is to enter from the underlying nozzle of kitty cracker after light cycle oil light fraction and the heavy distillat mixing after hydrogenation.It is wherein light
The same embodiment of hydroconversion condition of the heavy distillat of recycle oil.The same embodiment of operating condition of kitty cracker.
Comparative example 2
Medium-sized tester and catalyst are identical with embodiment.Light cycle oil is cut without boiling range, and full fraction is direct
Hydrogenation plant is gone to be hydrogenated with, the full fraction of the light cycle oil after hydrogenation directly enters the underlying nozzle of kitty cracker.It is wherein light
The same embodiment of hydroconversion condition of the full fraction of recycle oil.The same embodiment of operating condition of kitty cracker.
Catalytic cracking product is distributed and hydrogen consumption is shown in Table 3.
Contrast comparative example 1 and comparative example 2 it is found that using boiling range cut method, can be obvious in hydrogenation process
Hydrogen consumption is reduced, hydrogen consumption is reduced to 2.6% from 4.3%.Although simultaneously it is found that products distribution makes moderate progress, being not very bright
It is aobvious.And comparative example and comparative example 2, then it is found that not only hydrogen consumption is reduced to 2.6% from 4.3%, and products distribution is obvious
Improve, when showing conversion per pass, gasoline yield increases to 64.5% from 58.9%；In addition octane number RON is increased to from 94.0
96.1.In addition, either embodiment or comparative example, even conversion per pass, also it is seen that the inventive method has very
High gasoline yield.
Table 1HAC catalyst properties
2 raw material oil nature of table
| Raw oil title | Catalytic cracking light cycle oil |
| Density（20℃）, kg/m3 | 948.8 |
| Freezing point, DEG C | -24 |
| Aniline point, DEG C | <30 |
| 10% carbon residue, weight % | 0.37 |
| Mean molecule quantity | 187 |
| Boiling range, DEG C | |
| Initial boiling point | 190 |
| 5% | 213 |
| 10% | 222 |
| 30% | 247 |
| 50% | 272 |
| 70% | 303 |
| 90% | 348 |
| 95% | 363 |
| The end point of distillation | 369 |
| Mass spectrography quality is constituted, % | |
| Alkane | 10.7 |
| Total cycloalkane | 4.6 |
| Total aromatic hydrocarbons | 84.7 |
| Mononuclear aromatics | 31.7 |
| Double ring arene | 45.0 |
| Gross mass | 100.0 |
Table 3
| Embodiment 1 | Comparative example 1 | Comparative example 2 | |
| Hydrogen consumes, % | 2.6 | 2.6 | 4.3 |
| Product slates, weight % | |||
| Dry gas | 1.8 | 2.1 | 2.2 |
| Liquefied gas | 23.4 | 24.8 | 25.4 |
| Gasoline | 64.5 | 59.5 | 58.9 |
| Light diesel fuel | 8.4 | 10.8 | 10.9 |
| Heavy oil | 0.2 | 0.7 | 0.6 |
| Coke | 1.7 | 2.1 | 2.0 |
| It is total | 100.0 | 100.0 | 100.0 |
| Octane number | |||
| RON | 96.1 | 94.8 | 94.0 |
| MON | 84.2 | 82.8 | 82.1 |
Claims (16)
1. it is a kind of maximize gasoline production catalysis conversion method, it is characterised in that the method is made up of the following steps：
(1) catalytic cracking light cycle oil is cleaved obtains light fraction and heavy distillat；
(2) step (1) heavy distillat carries out hydrotreating reaction, hydrogen dividing potential drop in the presence of hydrogen and hydrotreating catalyst
10.0～25.0MPa, separates product and obtains being hydrogenated with heavy distillat；
(3) step (1) light fraction, step (2) hydrogenation heavy distillat enter riser separately through different spray nozzles layering
Reactor, carries out catalytic cracking reaction in the presence of catalytic cracking catalyst, separates catalytic cracking catalyst to be generated and reaction oil
Gas, wherein reaction oil gas are isolated to the product including gasoline, light cycle oil；Wherein underlying nozzle of the light fraction from riser
Into hydrogenation heavy distillat is entered from the upper strata nozzle of riser.
2. according to the method for claim 1, it is characterised in that step (3) is described light cycle oil return to step (1).
3. according to the method for claim 1, it is characterised in that the method also includes：Step (3) the catalytic cracking catalysis to be generated
Agent gained regeneration catalyzing Cracking catalyst Jing after stripping, regeneration returns riser reactor and recycles.
4. according to the method for claim 1, it is characterised in that the cutting temperature of the light cycle oil is 250～260 DEG C.
5. according to the method for claim 1, it is characterised in that the condition of step (2) described hydrotreating is reaction temperature
330～450 DEG C, volume space velocity 0.1～2.0 hour-1, 1000～2000Nm of hydrogen to oil volume ratio3/m3。
6. according to the method for claim 1, it is characterised in that the active metal group of step (2) described hydrotreating catalyst
Vib metals and/or group VIII base metal is selected from, is appointed in support selected from alumina, silicon dioxide, amorphous silica-alumina
One or more.
7. according to the method for claim 6, it is characterised in that the vib metals are molybdenum or/and tungsten, group VIII non-noble gold
Belong to for nickel or/and cobalt.
8. according to the method for claim 6, it is characterised in that the active metal component is selected from nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum
Or the combination of cobalt-molybdenum.
9. according to the method for claim 1, it is characterised in that in hydrogenation heavy distillat, two ring aromatic content is not more than 10 heavy %.
10. according to the method for claim 9, it is characterised in that in hydrogenation heavy distillat, two ring aromatic content is not more than 8 heavy %.
11. according to claim 1 method, it is characterised in that the riser reactor is isometrical riser reactor or reducing
Riser reactor.
12. according to claim 1 method, it is characterised in that the distance of upper and lower layer nozzle with control reaction oil gas two-layer spray
The time of staying in mouth distance is 0.01～3 second.
13. according to claim 2 method, it is characterised in that the distance of upper and lower layer nozzle with control reaction oil gas two-layer spray
The time of staying in mouth distance is 0.05～1 second.
14. according to claim 1 method, it is characterised in that the reaction condition of catalytic cracking unit is：Reaction temperature be 520～
650 DEG C, agent oil quality than 5～100, the 1-10 seconds oil gas time of staying, 0.15～0.4MPa of pressure, the weight of water vapour and raw material
Than for 0.01～0.5, Catalyst Balance Activity is not less than 65.
15. according to claim 14 method, it is characterised in that the reaction condition of catalytic cracking unit is：Reaction temperature is 550
～590 DEG C, than 8～50,2～8 seconds oil gas time of staying, water vapour are 0.02～0.2 with the weight ratio of raw material to agent oil quality, are urged
Agent equilibrium activity is not less than 68.
16. according to claim 1 method, it is characterised in that step (3) catalytic cracking catalyst includes zeolite, inorganic oxygen
Compound and optional clay, the content of each component are respectively：10～50 weight % of zeolite, 5～90 weight % of inorganic oxide, clay 0
～70 heavy %, wherein active component are selected from one or more of Y, HY, the USY or Beta zeolite with or without rare earth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310517650.9A CN104560186B (en) | 2013-10-28 | 2013-10-28 | Catalytic conversion method capable of realizing maximum gasoline production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310517650.9A CN104560186B (en) | 2013-10-28 | 2013-10-28 | Catalytic conversion method capable of realizing maximum gasoline production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104560186A CN104560186A (en) | 2015-04-29 |
| CN104560186B true CN104560186B (en) | 2017-03-22 |
Family
ID=53077275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310517650.9A Active CN104560186B (en) | 2013-10-28 | 2013-10-28 | Catalytic conversion method capable of realizing maximum gasoline production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104560186B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110551526B (en) * | 2018-05-30 | 2021-08-06 | 中国石油化工股份有限公司 | Processing method of catalytic cracking light cycle oil |
| CN110551527B (en) * | 2018-05-30 | 2021-08-06 | 中国石油化工股份有限公司 | Method for producing gasoline rich in aromatic hydrocarbon |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1310222A (en) * | 2000-02-22 | 2001-08-29 | 中国石油化工集团公司 | Petroleum hydrocarbon catalytic cracking process of producing diesel oil and high-octane number gasoline |
| CN1816609A (en) * | 2003-06-03 | 2006-08-09 | 巴西石油公司 | Process for the fluid catalytic cracking of mixed feedstocks of hydrocarbons from different sources |
| CN101191081A (en) * | 2006-11-30 | 2008-06-04 | 中国石油化工股份有限公司 | Catalytic conversion method for hydrocarbon oil raw material |
| CN101210200A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrogenation treatment and catalytic cracking combined process for residual oil |
| CN101531924A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
| TW201024400A (en) * | 2008-12-19 | 2010-07-01 | China Petrochemical Technology Co Ltd | A combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils |
| WO2011121613A2 (en) * | 2010-03-31 | 2011-10-06 | Indian Oil Corporation Ltd | A process for simultaneous cracking of lighter and heavier hydrocarbon feed and system for the same |
-
2013
- 2013-10-28 CN CN201310517650.9A patent/CN104560186B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1310222A (en) * | 2000-02-22 | 2001-08-29 | 中国石油化工集团公司 | Petroleum hydrocarbon catalytic cracking process of producing diesel oil and high-octane number gasoline |
| CN1816609A (en) * | 2003-06-03 | 2006-08-09 | 巴西石油公司 | Process for the fluid catalytic cracking of mixed feedstocks of hydrocarbons from different sources |
| CN101191081A (en) * | 2006-11-30 | 2008-06-04 | 中国石油化工股份有限公司 | Catalytic conversion method for hydrocarbon oil raw material |
| CN101210200A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrogenation treatment and catalytic cracking combined process for residual oil |
| CN101531924A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
| TW201024400A (en) * | 2008-12-19 | 2010-07-01 | China Petrochemical Technology Co Ltd | A combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils |
| WO2011121613A2 (en) * | 2010-03-31 | 2011-10-06 | Indian Oil Corporation Ltd | A process for simultaneous cracking of lighter and heavier hydrocarbon feed and system for the same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104560186A (en) | 2015-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104560185B (en) | The catalysis conversion method of aromatic compound gasoline is rich in a kind of production | |
| CN104560166B (en) | A kind of petroleum hydrocarbon is produced the catalysis conversion method of high-knock rating gasoline | |
| CN103013559B (en) | Hydrocracking method for selective increasing of aviation kerosene yield | |
| CN101519603B (en) | Method for hydrotreating high-sulfur and high-metal residual oil | |
| CN102399586B (en) | A mid-pressure hydrocracking method for producing jet fuel | |
| CN100389181C (en) | Production of intermediate fractional oil from Fischer-Tropsch synthetic oil | |
| CN104560187B (en) | The catalysis conversion method of aromatic type gasoline is rich in a kind of production | |
| JP6501898B2 (en) | Diesel fuel and jet fuel production system and method using Fischer-Tropsch synthetic oil | |
| CN101591562A (en) | A kind of fluidized catalytic cracking method and device thereof | |
| CN102041084A (en) | Heavy hydrocarbon hydrogenation combined process | |
| CN103923698B (en) | A kind of catalysis conversion method producing aromatics | |
| CN102344828B (en) | Processing method of inferior residual oil | |
| CN103059998B (en) | Combined process for treating residual oil | |
| CN101230291B (en) | Low consumption energy method for processing fischer-tropsch synthesis | |
| CN105754646B (en) | A kind of catalytic diesel oil hydro-conversion and gasoline hydrogenation integrated processes | |
| CN104560167B (en) | A kind of catalysis conversion method of hydrocarbon ils | |
| CN100395315C (en) | Hydrogenation purifying combined process for Fischer-Tropsch synthetic substance | |
| CN101962572A (en) | Coal tar heavy fraction fluidized-bed hydrocracking method and system thereof | |
| CN107557064B (en) | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation | |
| CN104560186B (en) | Catalytic conversion method capable of realizing maximum gasoline production | |
| CN103773473A (en) | Two-stage hydrocracking method used for producing high-quality jet fuel | |
| CN103059997A (en) | Combined technique of hydrotreating and delay coking of residual oil | |
| CN103923699B (en) | A kind of catalysis conversion method of producing high-knock rating gasoline | |
| CN104560184B (en) | A kind of catalysis conversion method of voluminous gasoline | |
| CN101376826B (en) | Hydrogenation technological process for long distillate coking kerosene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |