CN102079996B - Catalytic conversion method for producing high-quality light fuels from crude oil - Google Patents
Catalytic conversion method for producing high-quality light fuels from crude oil Download PDFInfo
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Abstract
The invention discloses a catalytic conversion method for producing high-quality light fuels from crude oil. The crude oil contacts and reacts with a catalyst which is rich in mesoporous zeolite and in coarse particle size distribution. The catalytic conversion method is characterized in that a reaction product containing catalytic wax oil which accounts for 12-60 wt% of the weight of raw material is obtained by the reaction temperature, weight hourly space velocity and the weight ratio of raw oil to catalyst, wherein the reaction temperature is 420-600 DEG C, the weight hourly space velocity is 25-100 hours<-1>, the weight ratio of catalyst to raw oil is 1 to 30, and the wax is catalyzed before hydrocracks. In the invention, crude oil catalytic converter and hydrocracking methods are provided, which, in particular, reduces dry gas and coke yield significantly while converting the poor quality of crude oil into high octane gasoline and high-cetane diesel fuel so as to achieve efficient use of oil resources, and reduce the broken tendency of the catalyst and the catalyst consumption.
Description
Technical field
The present invention relates to a kind of method of crude oil catalyzed conversion and hydrocracking combinations produce high-quality light Fuel.More specifically, be the method for producing substantially stop bracket gasoline and high hexadecane value diesel oil by catalyzed conversion and hydrocracking.
Background technology
Demand to high-quality diesel oil in worldwide increases day by day, and the demand of oil fuel is day by day reduced.Although vapour, diesel oil increase in demand is with from different places and different, generally worldwide will be over to gasoline demand rate of growth to the rate of growth of diesel oil demand.Therefore, more low-cetane catalysis solar oil is just being used as the blend component of diesel oil.And in order to meet the demand of high-quality diesel oil, need to carry out upgrading to catalysis solar oil, or directly by catalytic cracking (FCC), produce a large amount of high-quality catalysis solar oils.
The production of catalytically cracked gasoline and diesel oil is generally take straight run vacuum distillate (VGO) as raw material and mix refining part residual oil as long residuum (AR), vacuum residuum (VR) etc.The heavy metal content such as the contained carbon residue of the heavy feed stocks such as residual oil, sulphur, nitrogen, nickel, vanadium are high.For improving the character of these catalytic cracking unit (FCCU) charging, except by delayed coking or diasphaltene etc. to its decarburization, demetalization, the increasing employing of catalytic cracking makes FCCU stock oil increase hydrogen depickling demetalization to heavy oil, residual hydrogenation, further fully efficiently utilizes crude oil.The hydro-upgrading hydrogen-consuming volume of FCCU charging is large, limited by hydrogen source, and FCCU charging hydrogenation can not overcome the drawback that in conventional riser catalytic cracking process, sedimentation of coke causes catalyst activity and selectivity to decline.Inherent defect for riser reactor, US4243514, US4263128 have disclosed the method for crude oil full-fraction or part fraction upgrading, employing is without inert heat carrier material absorption crude oil full-fraction or the part cut of cracking activity, to remove carbon residue and the heavy metal in raw material, the raw material after upgrading is re-used as the charging of conventional FCCU and carries out cracking.But there is many drawbacks such as gasoline property is poor, energy consumption is high in the method.
Generally speaking, existing light fractions of FCC naphtha olefin(e) centent is high, thus the last running part octane value quality of gasoline that affects on the low side; Catalytic cracking diesel oil contains more mononuclear aromatics, and cetane value is low, second-rate.In order to meet the demand of growing motor spirit, be necessary to develop a kind of catalysis conversion method that heavy feed stock is converted into the high-quality light Fuels such as stop bracket gasoline and high hexadecane value diesel oil and rocket engine fuel.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of catalysis conversion method of producing high-quality light fuels from crude oil.
The catalysis conversion method of producing high-quality light fuels from crude oil provided by the invention comprises:
In catalytic conversion reactor, the pre-treatment crude oil of take contacts and reacts with catalyzer containing the thick size distribution of large pore zeolite as stock oil in reactor, it is characterized in that temperature of reaction, the oil gas residence time, catalyzer are enough to make to react obtain comprising the reaction product that accounts for stock oil 12～60 heavy % catalytic wax oil with stock oil weight ratio, wherein said weight hourly space velocity is 25～100h
-1, described temperature of reaction is 420～600 ℃, described catalyzer and stock oil weight ratio are 1～30.Catalytic wax oil is further hydrocracking again.
Described temperature of reaction is 420～600 ℃, preferably, and 450～550 ℃, more preferably, 460～520 ℃.
Described weight hourly space velocity is 30～80h
-1, preferably, 40～60h
-1.
The weight ratio of described catalyzer and stock oil is 1～30, preferably, and 2～25, more preferably, 3～14.
In embodiments, reaction pressure is 0.10MPa～1.0MPa.
Crude oil of the present invention is selected from or comprises in petroleum base crude oil and/or other mineral oil the mixture of one or more (comprise two kinds, lower with), and other mineral oil is one or more the mixture in liquefied coal coil, tar sand oil, shale oil.
The preprocessing process of crude oil of the present invention refers to the processes such as conventional crude oil desalting, dehydration, decalcification, through said process, removes most salts substances (as magnesium chloride, sodium-chlor etc.), water and calcium etc. in crude oil.In crude oil after pretreatment of the present invention, vanadium, nickel total value are preferably not more than 30ppm, and its density (20 ℃) is greater than 0.85gcm
-3, be preferably greater than 0.90gcm
-3, more preferably greater than 0.92gcm
-3.
In preferred embodiments, described crude oil is selected from or comprises petroleum base crude oil, comprise paraffinic crude, paraffin-intermediate base crude oil, Medium-paraffin base crude oil, intermediate base crude oil, in one or more in m-naphthenic base crude, cycloalkanes-intermediate base crude oil, naphthenic base crude.Most preferred crude oil is petroleum base crude oil, more preferably contains the heavy crude base crude oil of at least 1 % by weight pitch composition.
In embodiments, described catalyzer comprises zeolite, inorganic oxide and optional clay, and each component accounts for respectively total catalyst weight: the heavy % of zeolite 1～50, the heavy % of inorganic oxide 5～99, the heavy % of clay 0～70.Its mesolite is large pore zeolite and/or optional mesopore zeolite, and large pore zeolite accounts for 80～100 heavy % of zeolite gross weight, preferably the heavy % of 90 heavy %-100; Mesopore zeolite accounts for 0～20 heavy % of zeolite gross weight, preferably the heavy % of 0 heavy %-10.Large pore zeolite is selected from Y-series zeolite, comprises super steady Y, high silicon Y that Rare Earth Y (REY), rare earth hydrogen Y (REHY), different methods obtain.Mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, also can carry out modification to the transition metal such as the non-metallic elements such as phosphorus and/or iron, cobalt, nickel for above-mentioned mesopore zeolite, the more detailed description of relevant ZRP is referring to US5,232,675, ZSM series zeolite is selected from one or more the mixture among the zeolite of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other similar structures, the more detailed description of relevant ZSM-5 is referring to US3,702,886.
Inorganic oxide, as caking agent, is selected from silicon-dioxide (SiO
2) and/or aluminium sesquioxide (Al
2o
3).In butt, in inorganic oxide, silicon-dioxide accounts for the heavy % in 50 heavy～90, aluminium sesquioxide accounts for 10 heavy～50 heavy %.
Clay, as matrix (being carrier), is selected from one or more in silicon-dioxide, kaolin and/or halloysite, polynite, diatomite, halloysite, saponite, rectorite, sepiolite, attapulgite, hydrotalcite, wilkinite.Catalytic converting catalyst in each reactor can be identical, also can be different.
The size composition of the catalyzer of described thick size distribution is: be less than volume ratio that the particle of 40 microns accounts for all particles lower than 10%, be preferably lower than 5%; Be greater than volume ratio that the particle of 80 microns accounts for all particles lower than 15%, be preferably lower than 10%, all the other are the particle of 40～80 microns.
In a more preferred embodiment, described reactor be selected from riser tube, etc. one or more the combination in the fluidized-bed, isodiametric fluidized-bed, upstriker transfer limes, downstriker transfer limes of linear speed, or the two or more combinations of same reactor, described combination comprises series connection or/and in parallel, and wherein riser tube is the isodiametric riser tube of routine or the riser tube of various forms reducing.
In a more preferred embodiment, a position, described stock oil is introduced in reactor, or in the position of more than one identical or different height, described stock oil is introduced in reactor.
In a more preferred embodiment, described method also comprises carries out reaction product and catalyzer separated, and catalyzer is Returning reactor after stripping, coke burning regeneration, and the product after separation comprises stop bracket gasoline, high hexadecane value diesel oil and catalytic wax oil.
In a more preferred embodiment, described catalytic wax oil is that initial boiling point is not less than the cut of 330 ℃.
In a more preferred embodiment, described catalytic wax oil hydrogen richness is not less than 11.5 heavy %, is preferably not less than 12 heavy %.
Catalytic wax oil hydrocracking is under hydrogen exists situation, contacts, at reaction pressure 4.0～16.0MPa, 280～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～2000v/v, volume space velocity 0.1～10.0h with hydrocracking catalyst
-1reaction conditions under to carry out hydrocracking resulting.Hydrocracking tail oil can return to catalytic convention design as stock oil.
Catalytic wax oil hydrocracking catalyst contains one or more active metal components in W, Mo, Ni and Co, and acid cracking component.In hydrocracking catalyst, the weight content of active metal component in catalyzer is generally 5～50%, is generally 15～30%.Hydrocracking catalyst is for producing the intermediate distillates type hydrocracking catalyst of intermediate oil.Acid cracking activity component is generally selected from molecular sieve and amorphous silicon aluminium, and the molecular sieve type often using has: Y zeolite, beta molecular sieve, type ZSM 5 molecular sieve, SAPO Series Molecules sieve, etc.In hydrocracking catalyst, can also contain other refractory inorganic oxides, as the composite oxides of aluminum oxide, silicon oxide, titanium oxide and various elements or mixed oxide etc. simultaneously.
The preparation method of catalytic wax oil hydrocracking catalyst comprises molecular sieve and carrier preparation.The preparation of molecular sieve comprises the synthetic and modification of molecular sieve, and modification mainly contains metallic cation exchange, hydrothermal treatment consists, liquid phase chemical modification, gas chemistry modification etc.Carrier be prepared with extrusion method and coprecipitation method.
Preferred forms of the present invention is to carry out in a kind of reducing riser reactor, about the more detailed description of this reactor referring to CN1237477A.
In another embodiment of the invention, provide a kind of catalysis conversion method that the pretreated crude oil such as desalination, dehydration are stock oil of take, wherein stock oil contacts with the catalyzer that is rich in large pore zeolite and reacts in reactor, it is characterized in that:
(1) stock oil comprises difficult cracking stock oil and easy cracking stock oil, a position, described stock oil is introduced in reactor, or in the position of more than one identical or different height, described stock oil is introduced in reactor;
(2) difficult cracking stock oil in reactor first be rich in the catalyzer contact reacts of the thick size distribution of large pore zeolite, or be not later than easy cracking stock oil and react;
(3) temperature of reaction, weight hourly space velocity, catalyzer are enough to make to react obtain comprising the reaction product that accounts for stock oil 12～60 heavy % catalytic wax oil with stock oil weight ratio;
(4) reclaimable catalyst is separated by cyclonic separator with reaction oil gas; Optionally, reclaimable catalyst enters stripper, Returning reactor after stripping, coke burning regeneration; Reaction oil gas is isolated to the reaction product that comprises stop bracket gasoline, high hexadecane value diesel oil, catalytic wax oil;
(5) wherein catalytic wax oil, through hydrocracking, obtains gasoline, high hexadecane value diesel oil and hydrogenation heavy oil, and described hydrogenation heavy oil is oily or/and easy cracking stock oil turns back to step (1) or/and in step (2) as difficult cracking stock.
Described difficult cracking stock grease separation from or comprise that density (20 ℃) is greater than 0.90gcm
-3be preferably greater than 0.92gcm
-3more preferably greater than 0.93gcm
-3crude oil with poor quality, slurry oil, diesel oil, gasoline in one or more mixture.Described gasoline is selected from or comprises a kind of in present method gained catalytically cracked gasoline, the catalytically cracked gasoline from outside this device, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline, hydrogenated gasoline or more than one mixture wherein, and wherein catalytically cracked gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline, hydrogenated gasoline are from the gasoline outside this device.Described diesel oil is selected from or comprises a kind of in present method gained catalytic cracking diesel oil, catalytic cracking diesel oil, straight-run diesel oil, coker gas oil, thermally splitting diesel oil, hydrogenated diesel oil or more than one mixture wherein, and wherein catalytic cracking diesel oil, straight-run diesel oil, coker gas oil, thermally splitting diesel oil, hydrogenated diesel oil are from the diesel oil outside this device.
Described easy cracking stock grease separation from or comprise through the pretreated petroleum base crude oil of routine and/or other mineral oil.Wherein petroleum base oil density (20 ℃) is greater than 0.85gcm
-3, but not higher than 0.90gcm
-3, can be selected from paraffinic crude, paraffin-intermediate base crude oil, Medium-paraffin base crude oil, intermediate base crude oil, in one or more mixture in m-naphthenic base crude, cycloalkanes-intermediate base crude oil, naphthenic base crude; Other mineral oil is one or more the mixture in liquefied coal coil, tar sand oil, shale oil.
The reaction conditions of difficult cracking stock oil is: 520～650 ℃ of temperature of reaction, weight hourly space velocity 100～800h
-1, reaction pressure 0.10～1.0MPa, catalyzer and difficult cracking stock oil weight ratio 30～150, the weight ratio of water vapor and difficult cracking stock oil is 0.05～1.0.
Easily the reaction conditions of cracking stock oil is: 420～550 ℃ of temperature of reaction, weight hourly space velocity 5～100h
-1, reaction pressure 0.10～1.0MPa, catalyzer and the easy weight ratio 1.0～30 of cracking stock oil, water vapor is 0.05～1.0 with the easy weight ratio of cracking stock oil.Preferably, easily the temperature of reaction of cracking stock oil is 450～540 ℃, and weight hourly space velocity is 10～90h
-1, be preferably 20～60h
-1.More preferably, easily the temperature of reaction of cracking stock oil is 460～520 ℃, weight hourly space velocity 30～50h
-1, catalyzer and stock oil weight ratio are 3～14.
In the present embodiment, the separation of catalyzer, reactor and reaction product etc. are identical with front a kind of embodiment.
The size composition of the catalyzer of described thick size distribution is: be less than volume ratio that the particle of 40 microns accounts for all particles lower than 10%, be preferably lower than 5%; Be greater than volume ratio that the particle of 80 microns accounts for all particles lower than 15%, be preferably lower than 10%, all the other are the particle of 40～80 microns.
In order to increase the agent-oil ratio of reaction catchment, improve the catalytic activity of catalyzer, can be by supplemental heat or cold regenerated catalyst, half regenerated catalyst, catalyzer, live catalyst to be generated.Cooling regenerated catalyst and half cooling regenerated catalyst are reclaimable catalyst cooling obtaining after two-stage regeneration and one section of regeneration respectively, regenerated catalyst carbon content is below 0.1 heavy %, be preferably below 0.05 heavy %, half regenerated catalyst carbon content is the 0.1 heavy % in heavy %～0.9, and preferably carbon content is the 0.15 heavy % in heavy %～0.7; Reclaimable catalyst carbon content is more than 0.9 heavy %, and preferably carbon content is the 0.9 heavy % in heavy %～1.2.
In a more preferred embodiment, described catalytic wax oil is that initial boiling point is not less than the cut of 330 ℃.
In a more preferred embodiment, described catalytic wax oil hydrogen richness is not less than 11.5 heavy %, is preferably not less than 12 heavy %.
Catalytic wax oil hydrocracking is under hydrogen exists situation, contacts, at reaction pressure 4.0～16.0MPa, 280～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～2000v/v, volume space velocity 0.1～10.0h with hydrocracking catalyst
-1reaction conditions under to carry out hydrocracking resulting.Hydrocracking tail oil can return to catalytic convention design as stock oil.
Catalytic wax oil hydrocracking catalyst contains one or more active metal components in W, Mo, Ni and Co, and acid cracking component.In hydrocracking catalyst, the weight content of active metal component in catalyzer is generally 5～50%, is generally 15～30%.Hydrocracking catalyst is for producing the middle oil type hydrocracking catalyst of intermediate oil.Acid cracking activity component is generally selected from molecular sieve and amorphous silicon aluminium, and the molecular sieve type often using has: Y zeolite, beta molecular sieve, type ZSM 5 molecular sieve, SAPO Series Molecules sieve, etc.In hydrocracking catalyst, can also contain other refractory inorganic oxides, as the composite oxides of aluminum oxide, silicon oxide, titanium oxide and various elements or mixed oxide etc. simultaneously.
This technical scheme organically combines the techniques such as the catalyzed conversion of desalted crude and catalytic wax oil hydrocracking, from desalted crude, produces to greatest extent light-weight fuel oil, and especially stop bracket gasoline and high hexadecane value diesel oil, efficiently utilize thereby realize petroleum resources.The present invention compared with prior art has following technique effect:
1, crude oil work flow provided by the present invention has been cancelled the equipment such as process furnace in conventional crude still-process and atmospheric and vacuum tower, can reduce facility investment and equipment anticorrosion expense.
2, in the present invention, pre-treatment crude oil, through catalyzed conversion, removes carbon residue to crude oil respond well, and does not produce the byproducts such as coke, pitch.
3, Crude Oil of the present invention is through catalyzed conversion, good to crude oil metal removal effect, and demetallization per can approach or reach more than 95%.Metal in crude oil especially heavy metal is deposited on catalyzer through fluidized catalytic conversion; And the present invention replaces part water vapor to promote medium with the light constituent in crude oil, can make catalyst distribution even, and on catalyzer, heavy metal at high temperature reacts with lighter hydrocarbons, heavy metal loss part is active, obtain passivation to a certain degree, thereby suppressed the deleterious effect of heavy metal on catalyzer, improved significantly yield of light oil, slurry oil productive rate reduces significantly, thereby petroleum resources utilising efficiency improves.
4, diesel yield increases significantly, and diesel cetane-number obviously improves.
5, in the situation that gasoline yield increases, gasoline octane rating improves significantly; And dry gas yied and coke reduce significantly.
6, the hydroeracking unit operational cycle is improved significantly.
7, catalyzer because of particle more even, thereby in regenerative process, local temperature distribution is also more even, catalyst breakage tendency also correspondingly reduces.
8, catalyst consumption reduces, and the catalyst content in slurry oil reduces.
Accompanying drawing explanation
Accompanying drawing is the basic procedure schematic diagram of the catalysis conversion method of producing high-quality light fuels from crude oil provided by the invention.
Embodiment
Below in conjunction with accompanying drawing, further illustrate method provided by the present invention, but the present invention is not therefore subject to any restriction.
Accompanying drawing is the basic procedure schematic diagram of the catalysis conversion method of producing high-quality light fuels from crude oil provided by the invention.
Below in conjunction with accompanying drawing, method provided by the present invention is further described, but the present invention is not therefore subject to any restriction.
Embodiments of the present invention are to carry out in a kind of reducing riser reactor, about the more detailed description of this reactor referring to CN1237477A.
Its technical process is as shown in drawings:
Pre-lift medium is entered by riser reactor 2 bottoms through pipeline 1, from the regenerated catalyst of pipeline 16 under the castering action of pre-lift medium along the riser tube accelerated motion that makes progress, difficult cracking stock oil is the bottom with injecting lift pipe 2 reaction zone I together with atomizing steam from pipeline 4 through pipeline 3, mix with the existing logistics of riser reactor, there is cracking reaction in difficult cracking stock oil, and upwards accelerated motion on hot catalyzer.Easily cracking stock oil as low-density oil base crude oil through pipeline 5 middle and upper part with injecting lift pipe 2 reaction zone I together with atomizing steam from pipeline 6, mix with the existing logistics of riser reactor, there is cracking reaction in cracking stock oil easily on the lower catalyzer that contains certain charcoal, and upwards accelerated motion enters reaction zone II continuation reaction, the oil gas generating and the reclaimable catalyst of inactivation enter the cyclonic separator in settling vessel 8 through pipeline 7, realize the separated of reclaimable catalyst and oil gas, oil gas enters collection chamber 9, and catalyst fines returns to settling vessel by dipleg.In settling vessel, reclaimable catalyst flows to stripping stage 10, contacts with the steam from pipeline 11.The oil gas going out from stripping reclaimable catalyst enters collection chamber 9 after cyclonic separator.Reclaimable catalyst after stripping enters revivifier 13 through inclined tube 12, and main air enters revivifier through pipeline 14, and the coke on burning-off reclaimable catalyst makes the reclaimable catalyst regeneration of inactivation, and flue gas enters cigarette machine through pipeline 15.Catalyzer after regeneration enters riser tube through inclined tube 16.
Reaction product oil gas in collection chamber 9 is through main oil gas piping 17, enter follow-up separation system 18, the propylene that separation obtains is drawn through pipeline 102, the propane that separation obtains is drawn through pipeline 103, carbon four hydrocarbon are drawn through pipeline 104, catalytic cracked dry gas is drawn through pipeline 101, catalytically cracked gasoline is drawn through pipeline 105, according to need of production boiling range, be that the cut of 180～260 ℃ returns to riser tube 2 through pipeline 106 and also can be used as catalytic diesel oil output, boiling range is that the diesel oil distillate of 260～330 ℃ can be drawn through pipeline 107, also can draw through pipeline 108 and enter hydrocracking unit 19 together with catalytic wax oil (>=330 ℃), isolating light constituent draws through pipeline 201, hydrocracking light constituent can be used as light constituent according to need of production and separates and obtain rocket engine fuel, high hexadecane value diesel oil etc., also can be used as heavy constituent and through pipeline 202, return to the bottom of riser tube 2 reaction zone I together with hydrogenation heavy oil.
The following examples will be further described the present invention, but not thereby limiting the invention.The stock oil using in embodiment and comparative example is desalination, the pretreated crude oil that dewaters, and its character is listed in respectively table 1.
The catalytic converting catalyst preparation method who uses in embodiment is summarized as follows:
1), by 0.20kgNH
4cl is dissolved in 10kg water, in this solution, adds 1.0kg (butt) crystallization product ZRP-1 zeolite (Qilu Petrochemical Company's catalyst plant production, SiO
2/ Al
2o
3=30, content of rare earth RE
2o
3=2.0 heavy %), after 90 ℃ of exchange 0.5h, filter to obtain filter cake; Add 40gH
3pO
4(concentration 85%) and 45gFe (NO
3)
3be dissolved in 0.90kg water, dry with filter cake hybrid infusion; Then at 550 ℃ of roasting temperatures, process and within 2 hours, obtain phosphorous and MFI structure mesopore zeolite iron, its elementary analytical chemistry consists of
0.1Na
2O·5.1Al
2O
3·2.4P
2O
5·1.5Fe
2O
3·3.8RE
2O
3·88.1SiO
2。
2), configuration 200 liter silica concentrations are 155kg/m
3water glass solution and 100 liter free acids be 148kg/m
3, Al
2o
3content is 20kg/m
3acidified aluminum sulfate solution, above-mentioned two kinds of solution enter flash mixer reaction simultaneously, obtain silicon sol.
Kaolin slurry 45kg halloysite (Suzhou china clay company Industrial products, the heavy % of solid content 71.6) making beating being obtained with 25kg decationized Y sieve water; The above-mentioned silicon sol having prepared is mixed with kaolin slurry, pull an oar 1 hour.Add again 5.5kg pseudo-boehmite (Shandong Aluminum Plant's Industrial products, Al
2o
3content is 33 heavy %), and 45kg deionized water mixes making beating 30 minutes, then adding 2.5 liter concentration is hydrochloric acid (acid/Al of 31 heavy %
2o
3mol ratio is 0.2), its PH is adjusted to 2～4, stir, within standing aging 1 hour at 60～70 ℃, obtain silicon oxide-kaolin-aluminum oxide mixed sols.
3), by step 1) MFI structure mesopore zeolite (butt is 2.0kg) and DASY zeolite (Qilu Petrochemical Company's catalyst plant Industrial products of the phosphorous and iron prepared, lattice constant is 2.445～2.448nm, butt is 22.5kg) join step 2) in silicon oxide-kaolin-aluminum oxide mixed sols of obtaining, stir, spray drying forming, with ammonium dihydrogen phosphate (phosphorus content is 1m%) washing, wash away free Na
+be drying to obtain diameter and be the catalytic cracking catalyst sample of 20～120 microns, this catalyzer to consist of 2 heavy % phosphorous and MFI structure mesopore zeolite, 22 heavy %DASY zeolites, silica content iron be 32 heavy % pseudo-boehmites, 5 heavy % aluminium colloidal sol and surplus kaolin.
4) prepared catalyzer carries out aging through 800 ℃ and 100% water vapor, aging catalyst property is listed in table 2, its code name is MDCO-1, again aging dose of part is carried out to elutriation, remove fine particle and be greater than the particle of 100 microns, obtain the catalyzer of thick size distribution, its code name is MDCO-2, and its character is listed in table 2.
Catalytic wax oil hydrocracking catalyst HCC, the preparation of its carrier is by 75g pseudo-boehmite (Shandong Aluminum Plant's Industrial products, Al
2o
3content is 33 heavy %), 100gDASY zeolite (Qilu Petrochemical Company's catalyst plant Industrial products, lattice constant is 2.445-2.448nm, butt is 22.5kg), 5gH
3pO
4(concentration 85%) and suitable amount of adhesive etc. mix, extruded moulding, 120 ℃ of dry 3hr, and 500 ℃ of roasting 4hr, are ground into particle and obtain particulate state DASY-Al
2o
3carrier.Take ammonium metawolframate ((NH
4)
2w
4o
1318H
2o, chemical pure) and nickelous nitrate (Ni (NO
3)
218H
2o, chemical pure), water is made into 200mL solution.Solution is joined to DASY-Al
2o
3in 50 grams, carrier, at room temperature flood 3 hours, in steeping process, use ultrasonication steeping fluid 30 minutes, cooling, filter, be put in microwave oven and be dried approximately 15 minutes.Consisting of of this catalyzer: 30.0 heavy %WO
3, 3.1 heavy %NiO, 4.5 heavy %P
2o
5, 38 heavy % aluminum oxide and surplus SiO
2.The character of wax oil hydrogenation cracking catalyst HCC is listed in table 2.
Embodiment 1
The present embodiment explanation adopts method provided by the invention to carry out catalyzed conversion and hydrocracking reaction is produced a large amount of high-quality gasoline situations.
This embodiment tests according to the flow process of accompanying drawing, catalyzer is MDCO-2, stock oil A is directly oily as the easy cracking stock of catalytic cracking, on the middle-scale device by riser reactor, test, easily cracking stock oil enters I middle and upper part, reaction zone, and difficult cracking stock oil enters reaction zone I bottom.In reaction zone I bottom, difficult cracking stock oil is at 580 ℃ of temperature of reaction, weight hourly space velocity 240h
-1, the weight ratio 30 of catalytic cracking catalyst and difficult cracking stock oil, the weight ratio of water vapor and difficult cracking stock oil is under 0.20 condition, to carry out cracking reaction; In I middle and upper part, reaction zone, easily cracking stock oil is at 510 ℃ of temperature of reaction, weight hourly space velocity 90h
-1, catalytic cracking catalyst and the easily weight ratio 10 of cracking stock oil, water vapor is under 0.15 condition, to carry out cracking reaction with the weight ratio of easy cracking stock oil.At reaction zone II, reactant flow oil gas is at 495 ℃ of temperature of reaction, weight hourly space velocity 30h
-1, water vapor is under 0.15 condition, to carry out cracking reaction with the weight ratio of easy cracking stock oil.Reaction product oil gas is separated at settling vessel with catalyzer to be generated, product cuts by boiling range in separation system, thereby obtain propylene, gasoline, boiling range, is the catalytic wax oil that the cut of 180～250 ℃, diesel oil that boiling range is 250～330 ℃ and boiling range are greater than 330 ℃.Boiling range is that the cut of 180～250 ℃ is as oil circulation time catalytic convention design of easy cracking stock.Catalytic wax oil is carried out hydrocracking again, adopts hydrocracking catalyst HCC, and catalyzer is at hydrogen dividing potential drop 12.0MPa, 385 ℃ of temperature of reaction, hydrogen to oil volume ratio 1300v/v, volume space velocity 1.0h
-1reaction conditions under carry out hydrocracking, hydrogenation catalyst wax oil after hydrogenation cuts by boiling range, thereby the rocket engine fuel, the boiling range that obtain boiling range and be 180～250 ℃ are the diesel oil of 250～330 ℃ and are greater than the products such as hydrogenation catalyst wax oil cut of 330 ℃, the hydrogenation catalyst wax oil cut that is greater than 330 ℃ loops back above-mentioned medium-sized catalytic convention design, enters riser reactor reaction zone I bottom carry out cracking again as difficult cracking stock oil.Operational condition and product distribute and list in table 3.
As can be seen from Table 3, embodiment 1 Raw oil A is through catalyzed conversion, and catalytic wax oil productive rate is 31.58 heavy %, the heavy % of hydrogen richness 12.98, and nickel and vanadium are only 0.2 μ gg
-1, carbon residue is only 0.44 heavy %; Stock oil A is through catalyzed conversion and hydrocracking, and gasoline yield is 41.35 heavy %, and its research octane number (RON) (RON) is up to 91.48, and motor-method octane number (MON) is 85; Diesel yield is 26.05 heavy %, and cetane value is 56; The heavy % of jet fuel yield 17.74; The heavy % of lightweight oil total recovery 85.14.The heavy % of dry gas yield 1.01, the heavy % of coke yield 2.28.
Comparative example 1
Comparative example is to using stock oil A directly as the raw material of catalytic cracking, and the stock oil of test is identical with embodiment 1 with testing sequence and method, and the catalyzer just adopting changes catalyzer MDCO-1 into by the MDCO-2 of embodiment 1.Operational condition and product distribute and list in table 3.
As can be seen from Table 3, with respect to embodiment 1, the catalytic wax oil productive rate of comparative example 1 is low 0.98 heavy %, and its hydrogen richness low 0.12 heavy %, carbon residue exceeds 0.02 heavy %; And lightweight oil total recovery is low, be 84.13 heavy %; The heavy % of dry gas yied 1.25 and the heavy % of coke yield 2.98, dry gas and coke yield have significantly to be increased.
Embodiment 2
The present embodiment explanation adopts method provided by the invention to carry out catalyzed conversion and hydrocracking reaction is produced high-quality diesel oil situation in a large number.
This embodiment is identical with the testing apparatus of embodiment 1, using MDCO-2 as catalyzer, stock oil B is directly oily as the difficult cracking stock of catalyzed conversion, on the middle-scale device by riser reactor, test, difficult cracking stock oil enters the reaction of reaction zone I bottom, and easily cracking stock oil enters the reaction of I middle and upper part, reaction zone.In reaction zone I bottom, difficult cracking stock oil is at 520 ℃ of temperature of reaction, weight hourly space velocity 300h
-1, the weight ratio 90 of catalytic converting catalyst and difficult cracking stock oil, the weight ratio of water vapor and difficult cracking stock oil is under 0.20 condition, to carry out cracking reaction; In I middle and upper part, reaction zone, easily cracking stock oil is at 480 ℃ of temperature of reaction, weight hourly space velocity 120h
-1, catalytic converting catalyst and the easily weight ratio 30 of cracking stock oil, water vapor is under 0.15 condition, to carry out cracking reaction with the weight ratio of easy cracking stock oil; In addition, from stripping stage, supplement the steam stripped reclaimable catalyst of part and enter reaction zone II bottom, to reduce temperature and the reaction weight hourly space velocity of reaction zone II.At reaction zone II, oil gas is at 470 ℃ of temperature of reaction, weight hourly space velocity 20h
-1water vapor is under 0.15 condition, to carry out cracking reaction with the weight ratio of easy cracking stock oil, oil gas is separated at settling vessel with the catalyzer for the treatment of charcoal, product cuts by boiling range in separation system, thereby obtain propylene, part carbon four hydrocarbon and gasoline, boiling range is the catalytic wax oil of 330 ℃ of the diesel oil of 180～330 ℃ and boiling range >.Catalytic wax oil is carried out hydrocracking again, at hydrogen dividing potential drop 15.0MPa, 420 ℃ of temperature of reaction, hydrogen to oil volume ratio 1500v/v, volume space velocity 0.5h
-1reaction conditions under on catalyzer HCC, carry out hydrocracking, hydrogenation catalyst wax oil after hydrogenation cuts by boiling range, thereby obtain 150～240 ℃ rocket engine fuel, 240～330 ℃ diesel oil and be greater than hydrogenation catalyst wax oil cut of 330 ℃ etc., the hydrogenation catalyst wax oil cut that is greater than 260 ℃ loops back above-mentioned medium-sized catalytic convention design, enters I middle and upper part, catalytic convention design reaction zone carry out cracking again as easy cracking stock oil.Operational condition and product distribute and list in table 4.
As can be seen from Table 4, embodiment 2 Raw oil B are through catalyzed conversion, and catalytic wax oil productive rate is 40.23 heavy %, and nickel and vanadium are only 0.2 μ gg
-1, carbon residue is only 0.81 heavy %.After stock oil B catalyzed conversion and catalytic wax oil hydrocracking, diesel yield is 46.23 heavy %, and cetane value is 54; Gasoline yield is 29.12 heavy %, and its research octane number (RON) (RON) is up to 90.52, and motor-method octane number (MON) is 84; The heavy % of jet fuel yield 10.31; The heavy % of lightweight oil total recovery 85.66; The heavy % of dry gas yield 0.91; The heavy % of coke yield 2.79.
Comparative example 2
This comparative example is to using stock oil B directly as the difficult cracking stock of catalytic cracking, and the stock oil of test is identical with embodiment 2 with testing sequence and method, and the catalyzer just adopting changes catalyzer MDCO-1 into by the MDCO-2 of embodiment.Operational condition and product distribute and list in table 4.
As can be seen from Table 4, with respect to embodiment 2, comparative example 2 lightweight oil total recoverys are low, are 84.44 heavy %; The heavy % of dry gas yield 1.13; The heavy % of coke yield 3.58; Dry gas yied and coke yield have significantly to be increased.
Table 1
| Embodiment 1 comparative example 1 | Embodiment 2 comparative examples 2 | |
| Stock oil numbering | A | B |
| Stock oil character | ||
| Density (20 ℃), gcm -3 | 0.9010 | 0.9330 |
| Sulphur content, μ gg -1 | 8000 | 4300 |
| Nitrogen content, μ gg -1 | 4100 | 2100 |
| Aromatic hydrocarbons, heavy % | 12.5 | 31.2 |
| C, heavy % | 86.26 | 86.23 |
| H, heavy % | 12.20 | 12.69 |
| Carbon residue, heavy % | 6.4 | 7.2 |
| Metal content, μ gg -1 | ||
| Nickel | 26.0 | 18.7 |
| Vanadium | 1.0 | 1.2 |
| Sodium | 420 | 560 |
| Calcium | 78.5 | 80.4 |
| Acid number, mgKOHg -1 | 1.55 | 11.45 |
| Fractions consisting (ASTM D-1160) | ||
| IBP～200℃ | 7.5 | 2.5 |
| 200～350℃ | 17.6 | 9.0 |
| 350～500℃ | 27.5 | 27.0 |
| ＞500℃ | 47.4 | 61.5 |
Table 2
| Catalyzer | MDCO-1 | MDCO-2 | HCC |
| Particle diameter type | Conventional particle diameter | Coarse grain footpath | |
| Chemical constitution, heavy % | |||
| Aluminum oxide | 8.5 | 8.4 | 44 |
| Sodium oxide | 0.29 | 0.27 | ＜0.1 |
| Ferric oxide | 1.0 | 1.0 | - |
| Nickel oxide | - | - | 5.6 |
| Tungsten oxide 99.999 | - | - | 24.3 |
| Rare earth | 0.9 | 1.0 | - |
| Apparent density, kg/m 3 | 765 | 754 | 912 |
| Pore volume, ml/g | 0.28 | 0.26 | 0.35 |
| Specific surface area, rice 2/ gram | 117 | 114 | 326 |
| Abrasion index, heavy % hour -1 | 1.4 | 1.3 | 0.52 |
| Size composition, heavy % | |||
| 0～40 micron | 22.4 | 9.1 | - |
| 40～80 microns | 54.0 | 76.4 | - |
| 80 microns of > | 23.6 | 14.5 | - |
Table 3
| Embodiment 1 | Comparative example 1 | |
| Stock oil numbering | A | A |
| Catalytic conversion unit | ||
| Catalyzer | MDCO-2 | MDCO-1 |
| Outlet temperature of riser, ℃ | 490 | 490 |
| Riser reaction zone II | ||
| Temperature of reaction, ℃ | 500 | 500 |
| Weight hourly space velocity, h -1 | 20 | 20 |
| The weight ratio of water vapor/stock oil | 0.15 | 0.15 |
| Riser reaction zone I | ||
| Medial temperature, ℃ | 640/550 | 640/550 |
| Agent-oil ratio, m/m | 90/30 | 90/30 |
| Weight hourly space velocity, h -1 | 300/120 | 300/120 |
| The weight ratio of water vapor/stock oil | 0.20/0.15 | 0.20/0.15 |
| Catalytic wax oil | ||
| Yield, heavy % | 31.58 | 30.6 |
| Hydrogen richness, heavy % | 12.98 | 12.86 |
| Nickel+vanadium, μ gg -1 | 0.2 | 0.2 |
| Carbon residue, heavy % | 0.44 | 0.46 |
| Hydrocracking unit | ||
| Catalyzer | HCC | HCC |
| Hydrogen dividing potential drop, MPa | 18.0 | 18.0 |
| Temperature of reaction, ℃ | 450 | 450 |
| Hydrogen to oil volume ratio, v/v | 1500 | 1500 |
| Volume space velocity, h -1 | 0.5 | 0.5 |
| Product distributes, heavy % | ||
| Dry gas | 1.01 | 1.25 |
| Liquefied gas | 11.57 | 11.64 |
| Propylene and C 4 olefin | 4.38 | 4.37 |
| Gasoline | 41.35 | 41.25 |
| Rocket engine fuel | 17.74 | 17.42 |
| Diesel oil | 26.05 | 25.46 |
| Coke | 2.28 | 2.98 |
| Gasoline property | ||
| Research octane number (RON) RON | 91.48 | 91.56 |
| Motor-method octane number MON | 85 | 85 |
| Diesel oil character | ||
| Density (20 ℃), gcm -3 | 0.8152 | 0.8146 |
| Zero pour, ℃ | -4 | -4 |
| Cetane value | 56 | 56 |
Table 4
| Embodiment 2 | Comparative example 2 | |
| Stock oil numbering | B | B |
| Catalytic conversion unit | ||
| Catalyzer | MDCO-2 | MDCO-1 |
| Outlet temperature of riser, ℃ | 475 | 475 |
| Riser reaction zone II | ||
| Temperature of reaction, ℃ | 480 | 480 |
| Weight hourly space velocity, h -1 | 30 | 30 |
| The weight ratio of water vapor/stock oil | 0.15 | 0.15 |
| Riser reaction zone I | ||
| Medial temperature, ℃ | 550/510 | 550/510 |
| Agent-oil ratio, m/m | 60/10 | 60/10 |
| Weight hourly space velocity, h -1 | 180/60 | 180/60 |
| The weight ratio of water vapor/stock oil | 0.20/0.15 | 0.20/0.15 |
| Catalytic wax oil | ||
| Yield, heavy % | 40.23 | 38.56 |
| Hydrogen richness, heavy % | 11.84 | 11.67 |
| Nickel+vanadium, μ gg -1 | 0.2 | 0.2 |
| Carbon residue, heavy % | 0.81 | 0.84 |
| Hydrocracking unit | ||
| Catalyzer | HCC | HCC |
| Hydrogen dividing potential drop, MPa | 10.0 | 10.0 |
| Temperature of reaction, ℃ | 350 | 350 |
| Hydrogen to oil volume ratio, v/v | 500 | 500 |
| Volume space velocity, h -1 | 1.5 | 1.5 |
| Product distributes, heavy % | ||
| Dry gas | 0.91 | 1.13 |
| Liquefied gas | 10.64 | 10.85 |
| Propylene and C 4 olefin | 4.70 | 4.79 |
| Gasoline | 29.12 | 28.34 |
| Rocket engine fuel | 10.31 | 10.26 |
| Diesel oil | 46.23 | 45.84 |
| Coke | 2.79 | 3.58 |
| Gasoline property | ||
| Research octane number (RON) RON | 90.52 | 90.34 |
| Motor-method octane number MON | 84 | 83 |
| Diesel oil character | ||
| Density (20 ℃), gcm -3 | 0.8274 | 0.8268 |
| Zero pour, ℃ | -6 | -6 |
| Cetane value | 54 | 54 |
Claims (21)
1. the catalysis conversion method of producing high-quality light fuels from crude oil, it is characterized in that crude oil contacts and reacts with the catalyzer that contains the thick size distribution of large pore zeolite in reactor, it is characterized in that temperature of reaction, the oil gas residence time, catalyzer are enough to make to react obtain comprising the reaction product that accounts for stock oil 12～60 heavy % catalytic wax oil with stock oil weight ratio, wherein said weight hourly space velocity is 25～100h
-1, described temperature of reaction is 420～600 ℃, described catalyzer and stock oil weight ratio are 1～30; Catalytic wax oil is further hydrocracking again; Described large pore zeolite is selected from Y-series zeolite, comprise one or more in Rare Earth Y, rare earth hydrogen Y, super steady Y, high silicon Y, the size composition of the catalyzer of described thick size distribution is to be less than volume ratio that the particle of 40 microns accounts for all particles lower than 10%, is greater than volume ratio that the particle of 80 microns accounts for all particles lower than 15%; Described crude oil be selected from paraffinic crude, paraffin-intermediate base crude oil, Medium-paraffin base crude oil, intermediate base crude oil, in one or more in m-naphthenic base crude, cycloalkanes-intermediate base crude oil, naphthenic base crude; Described crude oil is through desalination, dehydration pre-treatment, and in the crude oil after processing, vanadium, nickel total value are not more than 30ppm, and its density is greater than 0.85g.cm
-3; Described catalyzer comprises zeolite, inorganic oxide and optional clay, each component accounts for respectively total catalyst weight: the heavy % of zeolite 1～50, the heavy % of inorganic oxide 5～99, the heavy % of clay 0～70, its mesolite is large pore zeolite and/or optional mesopore zeolite, and large pore zeolite accounts for 80-100 heavy % of zeolite gross weight.
2. according to the method for claim 1, it is characterized in that described temperature of reaction is 450～550 ℃, weight hourly space velocity is 30～80h
-1, the weight ratio of catalyzer and stock oil is 2～25.
3. according to the method for claim 2, it is characterized in that described temperature of reaction is 460～520 ℃, weight hourly space velocity is 40～60h
-1, the weight ratio of catalyzer and stock oil is 3～14.
4. according to the method for claim 1, the size composition that it is characterized in that the catalyzer of described thick size distribution is to be less than volume ratio that the particle of 40 microns accounts for all particles lower than 5%.
5. according to the method for claim 1, the size composition that it is characterized in that the catalyzer of described thick size distribution is to be greater than volume ratio that the particle of 80 microns accounts for all particles lower than 10%.
6. according to the method for claim 1, it is characterized in that described reactor be selected from riser tube, etc. one or more the combination in the fluidized-bed, isodiametric fluidized-bed, upstriker transfer limes, downstriker transfer limes of linear speed, or the two or more combinations of same reactor, described combination comprises series connection or/and in parallel, and wherein riser tube is the isodiametric riser tube of routine or the riser tube of various forms reducing.
7. according to the method for claim 1, it is characterized in that in described reactor, or in the position of more than one identical or different height, described stock oil is introduced in reactor.
8. according to the method for claim 1, it is characterized in that described method also comprises carries out separated by reaction product with catalyzer, catalyzer is Returning reactor after stripping, coke burning regeneration, and the product after separation comprises stop bracket gasoline, high hexadecane value diesel oil and catalytic wax oil.
9. according to the method for claim 1, it is characterized in that described catalytic wax oil is that initial boiling point is not less than the cut of 330 ℃, catalytic wax oil hydrogen richness is not less than 11.5 heavy %.
10. according to the method for claim 1, it is characterized in that catalytic wax oil hydrocracking is under hydrogen exists situation, contact with hydrocracking catalyst, at reaction pressure 4.0～16.0MPa, 280～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～2000v/v, volume space velocity 0.1～10.0h
-1reaction conditions react.
The catalysis conversion method of 11. producing high-quality light fuels from crude oils, is characterized in that the method comprises the following steps:
(1) stock oil comprises difficult cracking stock oil and easy cracking stock oil, a position, described stock oil is introduced in reactor, or in the position of more than one identical or different height, described stock oil is introduced in reactor;
(2) difficult cracking stock oil in reactor first be rich in the catalyzer contact reacts of the thick size distribution of large pore zeolite, or be not later than easy cracking stock oil and react;
(3) temperature of reaction, weight hourly space velocity, catalyzer are enough to make to react obtain comprising the reaction product that accounts for stock oil 12-60 heavy % catalytic wax oil with stock oil weight ratio;
(4) reclaimable catalyst is separated by cyclonic separator with reaction oil gas; Optionally, reclaimable catalyst enters stripper, Returning reactor after stripping, coke burning regeneration; Reaction oil gas is isolated to the reaction product that comprises stop bracket gasoline, high hexadecane value diesel oil, catalytic wax oil;
(5) wherein catalytic wax oil, through hydrocracking, obtains gasoline, high hexadecane value diesel oil and hydrogenation heavy oil, and described hydrogenation heavy oil is oily or/and easy cracking stock oil turns back to step (1) or/and in step (2) as difficult cracking stock;
Described large pore zeolite is selected from Y-series zeolite, comprise one or more in Rare Earth Y, rare earth hydrogen Y, super steady Y, high silicon Y, the size composition of the catalyzer of described thick size distribution is to be less than volume ratio that the particle of 40 microns accounts for all particles lower than 10%, is greater than volume ratio that the particle of 80 microns accounts for all particles lower than 15%.
12. according to the method for claim 11, it is characterized in that described difficult cracking stock grease separation certainly or comprises that density is greater than 0.90gcm
-3crude oil with poor quality, slurry oil, diesel oil, gasoline in one or more mixture.
13. according to the method for claim 11, it is characterized in that described easy cracking stock grease separation from or comprise paraffinic crude, paraffin-intermediate base crude oil, Medium-paraffin base crude oil, intermediate base crude oil, in one or more in m-naphthenic base crude, cycloalkanes-intermediate base crude oil, naphthenic base crude.
14. according to the method for claim 13, it is characterized in that described crude oil density after desalination, processed is not more than 0.90gcm
-3.
15. according to the method for claim 11, it is characterized in that the reaction conditions of difficult cracking stock oil is: 520～650 ℃ of temperature of reaction, weight hourly space velocity 100～800h
-1, reaction pressure 0.10～1.0MPa, catalyzer and difficult cracking stock oil weight ratio 30～150, the weight ratio of water vapor and difficult cracking stock oil is 0.05～1.0.
16. according to the method for claim 11, it is characterized in that the reaction conditions of easy cracking stock oil is: 420～550 ℃ of temperature of reaction, weight hourly space velocity 5～100h
-1, reaction pressure 0.10～1.0MPa, catalyzer and the easy weight ratio 1～30 of cracking stock oil, water vapor is 0.05～1.0 with the easy weight ratio of cracking stock oil.
17. according to the method for claim 11, and the temperature of reaction that it is characterized in that easy cracking stock oil is 450～540 ℃, and weight hourly space velocity is 10～90h
-1, catalyzer and stock oil weight ratio are 3～14.
18. according to the method for claim 12, and the temperature of reaction that it is characterized in that easy cracking stock oil is 460～520 ℃, weight hourly space velocity 30～50h
-1.
19. according to the method for claim 11, it is characterized in that described catalytic wax oil is that initial boiling point is not less than the cut of 330 ℃, and catalytic wax oil hydrogen richness is not less than 11.5 heavy %.
20. according to the method for claim 11, and the size composition that it is characterized in that the catalyzer of described thick size distribution is to be less than volume ratio that the particle of 40 microns accounts for all particles lower than 5%.
21. according to the method for claim 11, and the size composition that it is characterized in that the catalyzer of described thick size distribution is to be greater than volume ratio that the particle of 80 microns accounts for all particles lower than 10%.
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| CN101942340A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from inferior raw material oil |
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| CN102199447A (en) * | 2010-03-25 | 2011-09-28 | 中国石油化工股份有限公司 | Catalytic conversion method for producing high cetane value light diesel fuel and low olefine gasoline |
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| CN101942340A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from inferior raw material oil |
| CN102041093A (en) * | 2009-10-22 | 2011-05-04 | 中国石油化工股份有限公司 | Catalytic conversion method for improving cetane number and yield of diesel |
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