CN101724430B - Method for preparing light-weight fuel oil and propylene from inferior raw oil - Google Patents
Method for preparing light-weight fuel oil and propylene from inferior raw oil Download PDFInfo
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Abstract
The invention provides a method for preparing light-weight fuel oil and propylene from inferior raw oil. The method comprises the following steps that: the inferior raw oil enters a first and second reaction areas of a catalytic conversion reactor in sequence to contact the catalytic conversion catalyst to undergo the primary reaction and the secondary reaction, the reaction products and the spent catalyst undergo solid-liquid separation, and the spent catalyst undergoes steam stripping and singeing in sequence and then is returned to the reactor for recycling; the reaction products are separated to obtain propylene, gasoline, catalytic wax oil and other products, wherein the catalytic wax oil enters an aromatic extraction device for separation so as to obtain extract oil and raffinate oil; and the raffinate oil is cycled to the first reaction area of the catalytic conversion reactor or/and other catalytic conversion devices for further reaction to obtain the target products of propylene and gasoline. In the method, the inferior raw oil undergoes the mild catalytic conversion, the obtained catalytic wax oil undergoes aromatic extraction, and the extract oil richly contains double ring arenas and is a quite good chemically raw material; and the raffinate oil richly contains alkanes and naphthenic hydrocarbons, and is quite suitable for catalytic conversion, so that the highly efficient utilization of gasoline resources is realized.
Description
Technical field
The invention belongs to the catalysis conversion method of hydrocarbon ils, more particularly, is the method that inferior raw material is converted into a large amount of light-weight fuel oil and propylene by the combination of hydrocarbon oil catalytic cracking and arene extracting process process.
Background technology
Former oil quality is mainly manifested in oil density and becomes large along with the continuous increase of Oil extraction amount worse and worse, and viscosity uprises, and heavy metal content, sulphur content, nitrogen content, resin and asphalt content and acid number uprise.At present, the price difference of crude oil with poor quality and high-quality crude is along with the shortage of petroleum resources is also increasing, cause cheap crude oil with poor quality exploitation and working method more and more to receive publicity, that is to say, improve as much as possible the yield of lightweight oil from crude oil with poor quality, this has brought huge challenge for the processing technology of traditional crude oil.
Traditional heavy oil upgrading is divided into three class complete processings, and the first kind is hydrogenation technique, mainly comprises hydrotreatment and hydrofining; Equations of The Second Kind is decarbonization process, mainly comprises solvent deasphalting, delayed coking and heavy oil fluid catalytic cracking; The 3rd class is arene extracting process.Inferior heavy oil can improve hydrogen-carbon ratio by this three classes Technology, is lower boiling compound with the hydrocarbon conversion inferior.When inferior heavy oil adopts decarbonization process to process, sulphur in the inferior heavy oil, nitrogen and heavy metal content and aromatic hydrocarbons, resin and asphalt content are larger on the impact of decarbonization process, the decarbonization process existing problems are that liquid product yield is low, and product property is poor, need to process again.Resemble delay coking process, although impurity removal percentage is high, the green coke amount is more than 1.5 times of stock oil carbon residue, and how solid Jiao utilizes also is the problem that needs solution.Hydroprocessing technique can remedy the deficiency of decarbonization process, inferior heavy oil by hydrotreatment after, liquid product yield is high, product property is good, but that the hydrotreatment mode is often invested is larger.And arene extracting process have the investment little, repay fast characteristics, not only can reach good effect aspect the heavy oil processing, and the important industrial chemicals of by-product is aromatic hydrocarbons.
Patent CN100350020C discloses a kind of catalyzed cracking processing technique of inferior oil material, the method obtains poor quality oil through catalytic cracking solar oil cut Returning catalyticing cracking device freshening, the heavy oil fraction that obtains carries out solvent extraction, the heavy aromatics that extracts is as product, the Returning catalyticing cracking device freshening of raffinating oil.The method has solved the problem of heavy oil to a certain extent, but the method need be controlled the final boiling point of solar oil cut≤300 ℃, the final boiling point of heavy gas oil≤450 ℃, solar oil cut Returning catalyticing cracking device freshening wherein, heavy gas oil enters the aromatic extraction unit extracting, the Returning catalyticing cracking device of raffinating oil, although result's slurry oil amount decreases, but still relatively high, and do not have diesel product, dry gas output is also larger.
Patent CN100340643C discloses the treatment process of a kind of inferior heavy oil or residual oil, the method at first enters solvent extraction apparatus with heavy oil or residual oil raw material, the deasphalted oils that get enter the fixed bed hydrogenation treatment unit and carry out hydrotreatment more, the gained hydrogenation tail oil enters catalytic cracking unit, wherein the part or all of slurry oil of gained enters magnetic floating bed hydrogenation unit with obtained deasphalted oil by solvent extraction, product advances separation and obtains light ends and unconverted tail oil, and wherein unconverted tail oil is circulated to solvent extraction apparatus.The method is organically with catalytic cracking process, extraction process and hydrogenation technique combination, and processes at heavy oil certain effect is arranged, but the method technique boiling range is complicated, and liquid yield is low.
Along with the development of oil recovery technique, a large amount of peracid, high calcium crude oil are exploited out.Calcium contamination owner in the crude oil will be non-porphyrin organic calcium compound, only be dissolved in oil sulphur content, conventional desalting method can not separate these organic calcium compounds from crude oil, when the acid number in the crude oil surpasses 0.5mgKOH/g, will cause equipment corrosion, conventional atmospheric and vacuum distillation unit equipment is difficult to processing highly acid crude oil.For this reason, CN1827744A discloses a kind of method of processing crude oil with high acid value, the method is to make pretreated total acid value inject fluid catalytic cracking reactor greater than the crude oil of 0.5mgKOH/g after preheating to contact with catalyzer, and under the catalytic cracking reaction condition, react, oil gas behind the separating reaction and catalyzer, reaction oil gas is delivered to subsequent separation system, and reacted catalyzer recycles after stripping, regeneration.The method has that industrial applicibility is strong, running cost is low and the advantage such as deacidification effect is good, but dry gas and coke yield are higher, cause the benefit of utilizing of petroleum resources to reduce.
For a long time, those of ordinary skills think that the transformation efficiency of heavy oil fluid catalytic cracking is more high better.But the contriver through thinking creatively and repeatedly experiment find that the transformation efficiency of heavy oil fluid catalytic cracking is not more high better, when transformation efficiency high to a certain degree, the increase of purpose product seldom, the productive rate of dry gas and coke but increases considerably.
In order efficiently to utilize the inferior heavy oil resource, satisfy the demand of growing light-weight fuel oil, being necessary to develop a kind of is a large amount of lightweights and the catalysis conversion method of clean fuel oil with the inferior heavy oil feedstock conversion.
Summary of the invention
Technical problem to be solved by this invention is that the inferior heavy oil catalytic material is converted into a large amount of cleaning light-weight fuel oil and propylene.
Method of the present invention comprises the following steps:
(1), the first reaction zone that the inferior feedstock oil of preheating enters catalytic conversion reactor contacts the cracking reaction of generation macromole with the regeneration catalyzing conversion catalyst of heat, the oil gas that generates and used catalyst or with the second reaction zone that enters catalytic conversion reactor after the lightweight material oil that injects and/or cold shock medium mix, under certain reaction environment, carry out cracking reaction, hydrogen transfer reactions and isomerization reaction, after reaction product and the reaction with the reclaimable catalyst of charcoal after gas solid separation, reaction product enters separation system and is separated into dry gas, propylene, propane, the C4 hydrocarbon, gasoline, diesel oil and catalytic wax oil, reclaimable catalyst is transported to revivifier and carries out coke burning regeneration behind the water vapor stripping, the regenerated catalyst Returning reactor of heat recycles;
(2), described catalytic wax oil enters aromatic extraction unit, separate obtaining extracting oil out and raffinating oil;
(3), described the first reaction zone that is circulated to step (1) catalytic conversion reactor of raffinating oil obtains purpose product propylene and gasoline or/and other catalytic convention design is further reacted.
Technical scheme of the present invention is such implementation:
The inferior feedstock oil of preheating enters catalytic conversion reactor under the castering action of water vapor the first reaction zone contacts with the regeneration catalyzing conversion catalyst of heat, be 510 ℃～650 ℃ in temperature of reaction and be preferably 520 ℃～600 ℃, reaction times be preferably 0.1 second in 0.05 second～1.0 seconds～0.5 second, the weight ratio of catalyzer and stock oil (hereinafter to be referred as agent-oil ratio) is that 3～15:1 is preferably 4～12:1, the weight ratio of water vapor and stock oil (hereinafter to be referred as water-oil ratio) is that 0.03～0.3:1 is preferably 0.05～0.2:1, pressure is that the macromole cracking reaction occurs under the condition of 130kPa～450kPa, removes metal in the inferior feedstock oil, sulphur, nitrogen, at least a impurity in the naphthenic acid;
The oil gas that generates and used catalyst or with the second reaction zone that enters catalytic conversion reactor after the lightweight material oil that injects and/or cold shock medium mix, being 420 ℃～550 ℃ in temperature of reaction, to be preferably 460 ℃～530 ℃, reaction times be to be preferably 2 seconds in 1.5 seconds～20 seconds～to carry out cracking reaction, hydrogen transfer reactions and isomerization reaction under 10 seconds the condition; Reaction product isolated obtains dry gas, propylene, propane, C4 hydrocarbon, gasoline, diesel oil and catalytic wax oil, and wherein propane, C4 hydrocarbon, diesel oil also can be used as the lightweight material oil of described second reaction zone;
Described catalytic wax oil enters aromatic extraction unit, adopt existing arene extracting process to process, extract oil out as the industrial chemicals that is rich in aromatic hydrocarbons, the first reaction zone that is circulated to catalytic conversion reactor of raffinating oil obtains purpose product propylene and gasoline or/and other catalytic convention design is further reacted.
Other catalytic convention design is conventional catalytic cracking unit and various improved device thereof, and the description that preferably device is more detailed is referring to patent CN1232069A and CN1232070A.
Described inferior feedstock oil is heavy petroleum hydrocarbon and/or other mineral oil, and wherein heavy petroleum hydrocarbon is selected from one or more the mixture of arbitrary proportion in vacuum residuum (VR), inferior long residuum (AR), hydrogenated residue inferior, coker gas oil, deasphalted oil, crude oil with high acid value, the high metal crude oil; Other mineral oil is one or more in liquefied coal coil, tar sand oil, the shale oil.
Described inferior raw material oil properties satisfies a kind of in the following index at least:
Density is 900～1000 kg/ms
3, be preferably 930～960 kg/ms
3Carbon residue is that 4～15 heavy % are preferably 4～10 heavy %; Metal content is 15～600ppm, is preferably 15～100ppm; Acid number is 0.5～20mgKOH/g, is preferably 0.5～10.0mgKOH/g.
One or more in liquefied gas, gasoline, diesel oil of described lightweight material grease separation, described liquefied gas is from the liquefied gas of present method gained and/or the liquefied gas of other method gained; Described gasoline is selected from the gasoline of present method gained gasoline and/or other method gained; Described diesel oil is the diesel oil that is selected from present method gained diesel oil and/or other method gained.
Described catalytic wax oil is that the boiling range produced of this device or external device such as conventional catalytic cracking is greater than 200 ℃, more preferably greater than 300 ℃ catalytic wax oil.
Described raffinate oil be the boiling range produced of this device or this device and external device such as conventional catalytic cracking greater than 200 ℃, resulting through Aromatics Extractive Project more preferably greater than 300 ℃ catalytic wax oil.Raffinate oil as the stock oil of conventional catalytic cracking unit.
Described cold shock medium is one or more the mixture of arbitrary proportion in half regenerated catalyst, reclaimable catalyst and the live catalyst of the regenerated catalyst that is selected from cold shock agent, cooling, cooling, and wherein the cold shock agent is one or more the mixture of arbitrary proportion that is selected from liquefied gas, raw gasline, stable gasoline, diesel oil, heavy gas oil or the water; The regenerated catalyst of cooling and half regenerated catalyst of cooling are that reclaimable catalyst cools off after two-stage regeneration and one section regeneration respectively and obtains, the regenerated catalyst carbon content is below the 0.1 heavy %, be preferably below the 0.05 heavy %, half regenerated catalyst carbon content is the heavy % in 0.1 heavy %～0.9, and preferably carbon content is the heavy % in 0.15 heavy %～0.7; The reclaimable catalyst carbon content is more than the 0.9 heavy %, and preferably carbon content is the heavy % in 0.9 heavy %～1.2.
Described gasoline or diesel oil boiling range are adjusted according to actual needs, are not limited only to whole process gasoline or diesel oil.Described catalytic converting catalyst comprises zeolite, inorganic oxide and optional clay, and each component accounts for respectively total catalyst weight: the heavy % of zeolite 1 heavy %-50, the heavy % of inorganic oxide 5 heavy %-99, the heavy % of clay 0 heavy %-70.Its mesolite is as active ingredient, be selected from mesopore zeolite and/or optional large pore zeolite, mesopore zeolite accounts for the heavy % of 0 heavy %-100 of zeolite gross weight, the heavy % of preferred 20 heavy %-80, large pore zeolite accounts for the heavy % of 0 heavy %-100 of zeolite gross weight, the heavy % of preferred 20 heavy %-80.Mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, also can carry out modification with transition metals such as the non-metallic elements such as phosphorus and/or iron, cobalt, nickel to above-mentioned mesopore zeolite, the more detailed description of relevant ZRP is referring to US5,232,675, the 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.Large pore zeolite is selected from one or more the mixture in this group zeolite that the super steady Y that is obtained by Rare Earth Y (REY), rare earth hydrogen Y (REHY), different methods, high silicon Y consist of.
Inorganic oxide is selected from silicon-dioxide (SiO as caking agent
2) and/or aluminium sesquioxide (Al
2O
3).
Clay is selected from kaolin and/or halloysite as matrix (being carrier).
Described catalyzer also can be the employed useless equilibrium catalyst of conventional catalytic cracking unit.
Two reaction zones of catalytic cracking in the method can be suitable for the catalyzer of same type, also can be suitable for dissimilar catalyzer, and dissimilar catalyzer can be the different catalyzer of granular size and/or the different catalyzer of apparent bulk density.Active ingredient also can be selected respectively dissimilar zeolites on the different catalyzer of the catalyzer that granular size is different and/or apparent bulk density.Vary in size particle catalyzer and/or the height apparent bulk density catalyzer can enter respectively different reaction zones, for example, the oarse-grained catalyzer that contains ultrastable Y－type zeolite enters the first reaction zone, increase cracking reaction, the short grained catalyzer that contains rare earth Y type zeolite enters second reaction zone, increase hydrogen transfer reactions, the catalyzer that granular size is different is regenerated at same stripper stripping and same revivifier, then isolate macrobead and catalyst particle, catalyst particle enters second reaction zone through cooling.The catalyzer that granular size is different is to demarcate between 30～40 microns, and the catalyzer that apparent bulk density is different is with 0.6～0.7g/cm
3Between the boundary.
The applicable reactor of the method catalytic cracking unit can be selected from the equal diameter riser tube, etc. the linear speed riser tube, one of straighten in footpath riser tube or the fluidized-bed, also can be the compound reactor that is consisted of by equal diameter riser tube and fluidized-bed.Preferably select and straighten the compound reactor that footpath riser reactor or equal diameter riser tube and fluidized-bed consist of.
Described fluidized-bed reactor be selected from riser tube, etc. fluidized-bed, isodiametric fluidized-bed, upstriker transfer limes, one or both series combinations of downstriker transfer limes of linear speed.Riser tube can be conventional isodiametric riser tube, also can be the riser tube of various forms reducing.Wherein the gas speed of fluidized-bed is 0.1 meter per second-2 meter per second, and the gas speed of riser tube is 2 meter per seconds-30 meter per second (disregarding catalyzer).
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.
The method Aromatics Extractive Project unit is suitable for existing aromatic extraction unit.The solvent of described Aromatics Extractive Project is selected from one or more in furfural, methyl-sulphoxide, dimethyl formamide, monoethanolamine, ethylene glycol, the 1,2-PD, and temperature is 40～120 ℃, and the volume ratio of catalytic wax oil and solvent is 0.5～5.0:1.
This technical scheme organically combines the techniques such as catalytic cracking, Aromatics Extractive Project and conventional catalytic cracking, produces to greatest extent propylene and light-weight fuel oil from inferior raw material, stop bracket gasoline especially, thus realize that petroleum resources efficiently utilize.The present invention compared with prior art has following unforeseeable technique effect:
1, catalytic wax oil inferior is first through catalytic cracking, Aromatics Extractive Project then, thus the feedstock property of aromatic extraction unit improves significantly;
The stock oil character of 2, processing owing to aromatic extraction unit improves, thereby the aromatic extraction unit operational cycle is improved significantly;
3, catalytic wax oil inferior is after catalytic cracking, and resulting catalytic wax oil is extracted out in the oil and is rich in double ring arene through extracting, is good industrial chemicals.Raffinate oil and be rich in alkane and naphthenic hydrocarbon, be fit to very much carry out catalyzed conversion.
Description of drawings
Fig. 1 is the process flow diagram of embodiments of the present invention one.
Fig. 2 is the process flow diagram of embodiments of the present invention two.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Fig. 1 is the process flow diagram of embodiments of the present invention one, and in this embodiment, raffinating oil is circulated to the first reaction zone of the described catalytic conversion reactor of present method.
Its technical process is as follows:
The pre-lift medium is entered by riser reactor 2 bottoms through pipeline 1, from the regeneration catalyzing conversion catalyst of pipeline 16 under the castering action of pre-lift medium along the riser tube accelerated motion that makes progress, stock oil inferior through pipeline 3 with the bottom from the atomizing steam injecting lift pipe 2 reaction zone I of pipeline 4, mix with the existing logistics of riser reactor, cracking reaction occurs at the catalyzer of heat in inferior raw material, and upwards accelerated motion.Lightweight material oil through pipeline 5 with the bottom from the atomizing steam injecting lift pipe 2 reaction zone II of pipeline 6, mix with the existing logistics of riser reactor, cracking reaction occurs at the lower catalyzer that contains certain charcoal in lightweight material, and upwards accelerated motion, the oil gas that generates and the reclaimable catalyst of inactivation enter cyclonic separator in the settling vessel 8 through pipeline 7, the realization reclaimable catalyst separates with oil gas, and oil gas enters collection chamber 9, and catalyst fines returns settling vessel by dipleg.Reclaimable catalyst flows to stripping stage 10 in the settling vessel, contacts with steam from pipeline 11.The oil gas that stripping goes out from reclaimable catalyst enters collection chamber 9 behind cyclonic separator.Reclaimable catalyst behind the stripping enters revivifier 13 through inclined tube 12, and main air enters revivifier through pipeline 14, and the coke on the burning-off reclaimable catalyst makes the reclaimable catalyst regeneration of inactivation, and flue gas enters the cigarette machine through pipeline 15.Catalyzer after the regeneration enters riser tube through inclined tube 16.
Oil gas in the collection chamber 9 is through main oil gas piping 17, enter follow-up separation system 18, separating the propylene that obtains draws through pipeline 20, separating the propane that obtains draws through pipeline 21, and the C4 hydrocarbon is drawn through pipeline 22, propane and C4 hydrocarbon can be used as part lightweight material oil content is not circulated to above-mentioned catalytic convention design through pipeline 30 and 29 riser tube 2 reaction zone II, catalytic cracked dry gas is drawn through pipeline 19, gasoline fraction is drawn through pipeline 23, diesel oil distillate is drawn through pipeline 24, diesel oil distillate can be used as part lightweight material oil is circulated to above-mentioned catalytic convention design through pipeline 28 riser tube 2 reaction zone II, catalytic wax oil is transported to Aromatics Extractive Project unit 24 through pipeline 25, extracting oil out draws through pipeline 26, raffinate oil and be circulated to the riser tube 2 reaction zone I of above-mentioned catalytic convention design through pipeline 27, further produce low alkene stop bracket gasoline, propylene and diesel oil.
Fig. 2 is the process flow diagram of embodiments of the present invention two, and in this embodiment, raffinating oil is circulated to other catalytic convention design.The technical process of this embodiment and embodiment one basic identical, unique difference is to raffinate oil to enter another set of catalytic convention design 31 through pipeline 27, further produces low alkene stop bracket gasoline, propylene (not shown).
The following examples will be further described present method, but therefore not limit present method.
Used raw material is vacuum residuum, long residuum inferior, hydrogenated residue inferior and acid-containing raw oil among the embodiment, and its character is as shown in table 1.
Catalytic cracking catalyst GZ-1 preparation method used among the embodiment is summarized as follows:
1), with 20gNH
4Cl is dissolved in the 1000g water, adds 100g (butt) crystallization product ZRP-1 zeolite (production of Qilu Petrochemical Company catalyst plant, SiO in this solution
2/ Al
2O
3=30, content of rare earth RE
2O
3=2.0 heavy %), behind 90 ℃ of exchange 0.5h, filter to get filter cake; Add 4.0gH
3PO
4(concentration 85%) and 4.5gFe (NO
3)
3Be dissolved in the 90g water, dry with the filter cake hybrid infusion; Then process at 550 ℃ of roasting temperatures and obtained phosphorous and MFI structure mesopore zeolite iron in 2 hours, 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), use 250kg decationized Y sieve water with 75.4kg halloysite (Suzhou china clay company Industrial products, solid content 71.6m%) making beating, add again 54.8kg pseudo-boehmite (Shandong Aluminum Plant's Industrial products, solid content 63m%), with hydrochloric acid its PH is transferred to 2-4, stir, left standstill under 60-70 ℃ aging 1 hour, maintenance PH is 2-4, cools the temperature to below 60 ℃, add 41.5Kg aluminium colloidal sol (Qilu Petrochemical Company catalyst plant product, Al
2O
3Content is 21.7m%), stirred 40 minutes, obtain mixed serum.
3), with step 1) MFI structure mesopore zeolite (butt is 22.5kg) and DASY zeolite (the Qilu Petrochemical Company catalyst plant Industrial products of the phosphorous and iron of preparation, lattice constant is 2.445-2.448nm, butt is 2.0kg) join step 2) in the mixed serum that obtains, stir, spray drying forming, with ammonium dihydrogen phosphate (phosphorus content is 1m%) washing, the flush away Na that dissociates
+, being drying to obtain the catalytic cracking catalyst sample, consist of 15 heavy % MFI structure mesopore zeolite, 3 heavy %DASY zeolites, the 32 heavy % pseudo-boehmites, 6 phosphorous and iron of this catalyzer weigh % aluminium colloidal sol and surplus kaolin.
Hydrotreating catalyst preparation method used among the embodiment is summarized as follows: take by weighing 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 in alumina supporter 50 gram, at room temperature flooded 3 hours, used the ultrasonication steeping fluid 30 minutes in steeping process, cooling is filtered, and is put in the microwave oven dry about 15 minutes.Consisting of of this catalyzer: 30.0 heavy %WO
3, 3.1 heavy %NiO and surplus aluminum oxide.
Conventional catalytic cracking catalyst is respectively MLC-500 and CGP-1, and its character is listed in table 2.
Embodiment 1
This embodiment tests according to the flow process of Fig. 1, vacuum residuum feed A is as the raw material of catalytic cracking, middle-scale device at riser reactor is tested, inferior raw material enters reaction zone I bottom, contact with catalyzer GZ-1 and react, in reaction zone I bottom, raw material inferior is at 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.05 condition; At reaction zone II, oil gas mixes rear at 500 ℃ of temperature of reaction, weight hourly space velocity 30h with propane and C4 hydrocarbon, the diesel oil of circulation
-1The weight ratio of water vapor and raw material is to carry out cracking reaction under 0.05 condition, oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, product cuts by boiling range in separation system, thereby obtain dry gas, liquefied gas (comprises propylene, propane and C4 hydrocarbon, lower with), gasoline, diesel oil and greater than 330 ℃ catalytic wax oil, catalytic wax oil is through Aromatics Extractive Project, catalytic wax oil is 2 with the furfural ratio, extracting section temperature is 75 ℃, extract oil out as industrial chemicals, raffinating oil loops back above-mentioned kitty cracker.Operational condition and product distribute and list in table 3.
As can be seen from Table 3, total liquid yield is up to 82.01 heavy %, and wherein gasoline yield is up to 47.69 heavy %, productivity of propylene is up to 4.86 heavy %, and dry gas yied only is 2.48 heavy %, and the slurry oil productive rate only is 1.04 heavy %, obtains in addition the industrial chemicals that is rich in aromatic hydrocarbons of 7.06 heavy %.
Comparative Examples 1
This Comparative Examples is directly as the raw material of catalytic cracking with vacuum residuum feed A, test at the middle scale riser reactor assembly, it is 2.5 seconds in 500 ℃ of temperature of reaction, reaction times, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.05 condition; Oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, and product cuts by boiling range in separation system, thereby obtains dry gas, liquefied gas, gasoline, catalytic wax oil.Operational condition and product distribute and list in table 3.
As can be seen from Table 3, total liquid yield only is 77.44 heavy %, and wherein gasoline yield only is 43.76 heavy %, and productivity of propylene only is 4.21 heavy %, and dry gas yied weighs % up to 3.49, and the slurry oil productive rate is up to 9.18 heavy %.Compare with embodiment 1, Comparative Examples total liquid yield decrease causes the reduction of petroleum resources utilising efficiency.
This embodiment tests according to the flow process of Fig. 2, hydrogenated residue raw material C inferior is as the raw material of catalytic cracking, middle-scale device at riser reactor is tested, inferior raw material enters reaction zone I bottom, contact with catalyzer GZ-1 and react, in reaction zone I bottom, raw material inferior is at 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.05 condition; At reaction zone II, oil gas with after cooling regenerated catalyst as the cold shock medium mixes at 500 ℃ of temperature of reaction, weight hourly space velocity 30h
-1The weight ratio of water vapor and raw material is to carry out cracking reaction under 0.05 condition, oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, product cuts by boiling range in separation system, thereby obtain dry gas, liquefied gas and propylene, gasoline, diesel oil and greater than 330 ℃ catalytic wax oil, catalytic wax oil is through Aromatics Extractive Project, catalytic wax oil is 2 with the furfural ratio, and extracting section temperature is 75 ℃, extracts oil out as industrial chemicals, raffinate oil and enter the kitty cracker of another set of routine, adopt catalyzer CGP-1, at reaction zone I, 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalytic cracking catalyst and raw material, at reaction zone II, 500 ℃ of temperature of reaction, weight hourly space velocity 20h
-1, the weight ratio 6 of catalytic cracking catalyst and raw material is isolated dry gas, liquefied gas, gasoline, diesel oil and catalytic wax oil, and catalytic wax oil is returned aromatic extraction unit.Operational condition and product distribute and list in table 4.
As can be seen from Table 4, total liquid yield is up to 81.17 heavy %, and wherein gasoline yield is up to 38.03 heavy %, productivity of propylene is up to 7.64 heavy %, and dry gas yied only is 2.61 heavy %, and the slurry oil productive rate only is 1.23 heavy %, obtains in addition the industrial chemicals that is rich in aromatic hydrocarbons of 7.09 heavy %.
Comparative Examples 2
This Comparative Examples is directly as the raw material of catalytic cracking with hydrogenated residue raw material C inferior, test at the middle scale riser reactor assembly, adopt catalyzer CGP-1, it is 2.5 seconds in 500 ℃ of temperature of reaction, reaction times, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.10 condition; Oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, and product cuts by boiling range in separation system, thereby obtains dry gas, liquefied gas, gasoline, catalytic wax oil.Operational condition and product distribute and list in table 4.
As can be seen from Table 4, total liquid yield only is 77.29 heavy %, and wherein gasoline yield only is 33.04 heavy %, and productivity of propylene only is 7.06 heavy %, and dry gas yied weighs % up to 3.63, and the slurry oil productive rate is up to 9.77 heavy %.Compare with embodiment 2, Comparative Examples total liquid yield decrease causes the reduction of petroleum resources utilising efficiency.
This embodiment tests according to the flow process of Fig. 2, high-acid crude oil raw material E is as the raw material of catalytic cracking, middle-scale device at riser reactor is tested, inferior raw material enters reaction zone I bottom, contact with catalyzer GZ-1 and react, in reaction zone I bottom, raw material inferior is at 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.05 condition; At reaction zone II, oil gas is at 500 ℃ of temperature of reaction, weight hourly space velocity 30h
-1The weight ratio of water vapor and raw material is to carry out cracking reaction under 0.05 condition, oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, product cuts by boiling range in separation system, thereby obtain dry gas, liquefied gas and propylene, gasoline, diesel oil and greater than 330 ℃ catalytic wax oil, catalytic wax oil is through Aromatics Extractive Project, heavy cycle oil is 2 with the furfural ratio, and extracting section temperature is 75 ℃, extracts oil out as industrial chemicals, raffinate oil and enter the kitty cracker of another set of routine, adopt catalyzer CGP-1, at reaction zone I, 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalytic cracking catalyst and raw material, at reaction zone II, 500 ℃ of temperature of reaction, weight hourly space velocity 20h
-1, the weight ratio 6 of catalytic cracking catalyst and raw material is isolated dry gas, liquefied gas, gasoline, diesel oil and catalytic wax oil, and catalytic wax oil is returned aromatic extraction unit.Operational condition and product distribute and list in table 5.
As can be seen from Table 5, total liquid yield is up to 81.19 heavy %, and wherein gasoline yield is up to 36.93 heavy %, and productivity of propylene is up to 7.20 heavy %, and dry gas yied only is 3.01 heavy %, obtains in addition the industrial chemicals that is rich in aromatic hydrocarbons of 7.08 heavy %.
Comparative Examples 3
This Comparative Examples is directly as the raw material of catalytic cracking with high-acid crude oil raw material E, test at the middle scale riser reactor assembly, adopt catalyzer CGP-1, it is 2.5 seconds in 500 ℃ of temperature of reaction, reaction times, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.10 condition; Oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, and product cuts by boiling range in separation system, thereby obtains dry gas, liquefied gas, gasoline, catalytic wax oil.Operational condition and product distribute and list in table 5.
As can be seen from Table 5, total liquid yield only is 77.29 heavy %, and wherein gasoline yield only is 35.43 heavy %, and productivity of propylene only is 6.52 heavy %, and dry gas yied weighs % up to 5.51, and the slurry oil productive rate is up to 6.22 heavy %.Compare with embodiment 3, Comparative Examples total liquid yield decrease causes the reduction of petroleum resources utilising efficiency.
Embodiment 4～5
This embodiment tests according to the flow process of Fig. 2, long residuum B and crude oil with high acid value D are respectively as the raw material of catalytic cracking, middle-scale device at riser reactor is tested, inferior raw material enters reaction zone I bottom, contact with catalyzer GZ-1 and react, in reaction zone I bottom, raw material inferior is at 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalyzer and raw material, the weight ratio of water vapor and raw material are to carry out cracking reaction under 0.05 condition; At reaction zone II, oil gas is at 500 ℃ of temperature of reaction, weight hourly space velocity 30h
-1The weight ratio of water vapor and raw material is to carry out cracking reaction under 0.05 condition, oil gas separates at settling vessel with the catalyzer for the treatment of charcoal, product cuts by boiling range in separation system, thereby obtain dry gas, liquefied gas and propylene, gasoline, diesel oil and greater than 330 ℃ catalytic wax oil, catalytic wax oil is through Aromatics Extractive Project, catalytic wax oil is 2 with the furfural ratio, and extracting section temperature is 75 ℃, extracts oil out as industrial chemicals, raffinate oil and enter the kitty cracker of another set of routine, adopt catalyzer MLC-500, at reaction zone I, 600 ℃ of temperature of reaction, weight hourly space velocity 100h
-1, the weight ratio 6 of catalyzer and raw material, at reaction zone II, 500 ℃ of temperature of reaction, weight hourly space velocity 20h
-1, the weight ratio 6 of catalyzer and raw material is isolated dry gas, liquefied gas, gasoline, diesel oil and catalytic wax oil, and catalytic wax oil is returned aromatic extraction unit.Operational condition and product distribute and list in table 6.
As can be seen from Table 6, total liquid yield is respectively up to 77.29 heavy % and 78.76 heavy %, wherein gasoline yield is respectively up to 35.43 heavy % and 37.73 heavy %, productivity of propylene is respectively up to 6.52 heavy % and 4.82 heavy %, and dry gas yied only is respectively 5.51 heavy % and 2.69 heavy %, the slurry oil productive rate only is respectively 2.14 heavy % and 2.02 heavy %, obtains respectively in addition the industrial chemicals that is rich in aromatic hydrocarbons of 8.26 heavy % and 8.23 heavy %.
Table 1
| The stock oil title | Vacuum residuum | Vacuum residuum | Hydrogenated residue inferior | High-acid crude oil | High-acid crude oil |
| The stock oil code name | A | B | C | D | E |
| Density (20 ℃), kg/m 3 | 920.9 | 980 | 942.7 | 932.5 | 902.2 |
| Kinematic viscosity, millimeter 2/ second | |||||
| 80℃ | / | / | 137.7 | 156.45 | 52.5 |
| 100℃ | 114.4 | / | 62.78 | / | / |
| Carbon residue, heavy % | 8.2 | 13.95 | 8.0 | 6.7 | 7.89 |
| Condensation point, |
25 | / | / | / | / |
| Acid number, mgKOH/g | / | / | / | 12.52 | 3.62 |
| Total nitrogen, heavy % | 0.33 | 1.02 | / | / | 0.36 |
| Sulphur, heavy % | 0.21 | 1.39 | 0.24 | / | 0.14 |
| Carbon, heavy % | 86.91 | 85.35 | 87.82 | / | 86.33 |
| Hydrogen, heavy % | 12.55 | 11.14 | 12.07 | / | 12.66 |
| Metal content, ppm | |||||
| Nickel | 8.8 | 64.0 | 7.4 | 19.3 | 61.0 |
| Vanadium | 0.1 | 5.3 | 8.2 | 1.1 | 3.4 |
| Iron | 1.8 | / | 11.1 | / | 13.2 |
| Copper | <0.1 | / | / | / | / |
| Sodium | 3.0 | / | 1.2 | / | 43 |
| Calcium | 7.4 | 557 | 4.4 | ||
| Boiling range, ℃ | |||||
| Initial boiling point | 415 | / | 287 | / | / |
| 10％ | 545 | / | 394 | / | / |
| 30％ | / | / | 473 | / | / |
| 50％ | / | / | 558 | / | / |
| 70％ | / | / | / | / | / |
| 90％ | / | / | / | / | / |
| Final boiling point | / | / | / | / | / |
Table 2
| The catalyzer numbering | MLC-500 | GZ-1 | CGP-1 |
| Zeolite type | Large pore zeolite | Mesopore and large pore zeolite | Mesopore and large pore zeolite |
| Chemical constitution, heavy % | |||
| Aluminum oxide | 50.2 | 40.0 | 56.3 |
| Sodium oxide | 0.321 | 0.29 | 0.19 |
| Ferric oxide | / | 1.1 | / |
| Rare earth | 2.5 | 3.2 | |
| Apparent density, kg/m 3 | 700 | 750 | 630 |
| Pore volume, ml/g | 0.38 | 0.40 | 0.36 |
| Specific surface area, rice 2/ gram | 229 | 196 | 221 |
| Abrasion index is during heavy % -1 | 1.9 | 1.5 | 1.7 |
| Size composition, heavy % | |||
| 0～40 micron | 17.3 | 20.2 | 13.1 |
| 40～80 microns | 49.3 | 50.1 | 41.8 |
| 80 microns | 33.4 | 29.7 | 45.1 |
Table 3
| Embodiment 1 | Comparative Examples 1 | |
| The stock oil numbering | A | A |
| Reactor | The series connection riser tube | Riser tube |
| Catalytic cracking unit | ||
| Operational condition | ||
| Catalyzer | GZ-1 | / |
| Outlet temperature of riser, ℃ | 500 | / |
| Reaction zone I/II temperature, ℃ | 600/500 | / |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/25 | / |
| The weight ratio of water vapor/raw material | 0.05 | / |
| The Aromatics Extractive Project unit | ||
| Temperature, ℃ | 75 | / |
| Solvent | Furfural | / |
| Catalytic wax oil/ |
2 | / |
| Conventional catalytic cracking unit | ||
| Catalyzer | / | MLC-500 |
| Outlet temperature of riser, ℃ | / | 520 |
| Reaction zone I/II temperature, ℃ | / | / |
| Reaction zone I/II weight hourly space velocity, h -1 | / | 2.5 second |
| The weight ratio of water vapor/raw material | / | 0.05 |
| Product distributes, heavy % | ||
| Dry gas | 2.48 | 3.49 |
| Liquefied gas | 14.96 | 13.50 |
| Propylene | 4.86 | 4.21 |
| Gasoline | 47.69 | 43.76 |
| Diesel oil | 19.37 | 20.18 |
| Slurry oil | 1.04 | 9.18 |
| Coke | 7.41 | 9.89 |
| Extracting aromatic hydrocarbons | 7.06 | / |
| Add up to | 100.00 | 100.0 |
| Total liquid yield, heavy % | 82.01 | 77.44 |
| Gasoline octane rating | ||
| RON | 91.0 | 91.0 |
| MON | 79.8 | 78.1 |
Table 4
| |
Comparative Examples 2 | |
| The stock oil numbering | C | C |
| Reactor | The series connection riser tube | Riser tube |
| Catalytic cracking unit | ||
| Operational condition | ||
| Catalyzer | GZ-1 | / |
| Outlet temperature of riser, ℃ | 500 | / |
| Reaction zone I/II temperature, ℃ | 600/500 | / |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/25 | / |
| The weight ratio of water vapor/raw material | 0.05 | / |
| The Aromatics Extractive Project unit | ||
| Temperature, ℃ | 75 | / |
| Solvent | Furfural | / |
| Catalytic wax oil/ |
2 | / |
| Conventional catalytic cracking unit | ||
| Catalyzer | CGP-1 | CGP-1 |
| Outlet temperature of riser, ℃ | 500 | 500 |
| Reaction zone I/II temperature, ℃ | 600/500 | |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/20 | 2.5 second |
| The weight ratio of water vapor/raw material | 0.10 | 0.10 |
| Product distributes, heavy % | ||
| Dry gas | 2.51 | 3.63 |
| Liquefied gas | 21.17 | 20.17 |
| Propylene | 7.64 | 7.06 |
| Gasoline | 38.03 | 33.04 |
| Diesel oil | 21.97 | 24.08 |
| Slurry oil | 1.23 | 9.77 |
| Extracting aromatic hydrocarbons | 7.09 | / |
| Coke | 8.00 | 9.31 |
| Add up to | 100.00 | 100.0 |
| Total liquid yield, heavy % | 81.17 | 77.29 |
| Gasoline octane rating | ||
| RON | 94.5 | 94.0 |
| MON | 83.7 | 83.1 |
Table 5
| |
Comparative Examples 3 | |
| The stock oil numbering | E | E |
| Reactor | The series connection riser tube | Riser tube |
| Catalytic cracking unit | ||
| Operational condition | ||
| Catalyzer | GZ-1 | / |
| Outlet temperature of riser, ℃ | 500 | / |
| Reaction zone I/II temperature, ℃ | 600/500 | / |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/25 | / |
| The weight ratio of water vapor/raw material | 0.05 | / |
| The Aromatics Extractive Project unit | ||
| Temperature, ℃ | 75 | / |
| Solvent | Furfural | / |
| Catalytic wax oil/ |
2 | / |
| Conventional catalytic cracking unit | ||
| Catalyzer | CGP-1 | CGP-1 |
| Outlet temperature of riser, ℃ | 500 | 500 |
| Reaction zone I/II temperature, ℃ | 600/500 | |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/20 | 2.5 second |
| The weight ratio of water vapor/raw material | 0.10 | 0.10 |
| Product distributes, heavy % | ||
| Dry gas | 3.01 | 5.51 |
| Liquefied gas | 20.52 | 19.10 |
| Propylene | 7.20 | 6.52 |
| Gasoline | 36.93 | 35.43 |
| Diesel oil | 23.74 | 22.76 |
| Slurry oil | / | 6.22 |
| Oxygenatedchemicals | 0.75 | 0.82 |
| Extracting aromatic hydrocarbons | 7.08 | |
| Coke | 7.97 | 10.16 |
| Add up to | 100.00 | 100.00 |
| Total liquid yield, heavy % | 81.19 | 77.29 |
| Gasoline octane rating | ||
| RON | 91.0 | 90.0 |
| MON | 80.0 | 78.8 |
Table 6
| Embodiment 4 | Embodiment 5 | |
| The stock oil numbering | B | D |
| Reactor | The series connection riser tube | The series connection riser tube |
| Catalytic cracking unit | ||
| Operational condition | ||
| Catalyzer | GZ-1 | GZ-1 |
| Outlet temperature of riser, ℃ | 500 | 500 |
| Reaction zone I/II temperature, ℃ | 600/500 | 600/500 |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/25 | 100/25 |
| The weight ratio of water vapor/raw material | 0.05 | 0.05 |
| The Aromatics Extractive Project unit | ||
| Temperature, ℃ | 75 | 75 |
| Solvent | Furfural | Furfural |
| Catalytic wax oil/ |
2 | 2 |
| Conventional catalytic cracking unit | ||
| Catalyzer | MLC-500 | MLC-500 |
| Outlet temperature of riser, ℃ | 500 | 500 |
| Reaction zone I/II temperature, ℃ | 600/500 | 600/500 |
| Reaction zone I/II weight hourly space velocity, h -1 | 100/20 | 100/20 |
| The weight ratio of water vapor/raw material | 0.05 | 0.05 |
| Product distributes, heavy % | ||
| Dry gas | 2.69 | 2.81 |
| Liquefied gas | 12.63 | 12.88 |
| Propylene | 4.82 | 4.05 |
| Gasoline | 37.73 | 41.52 |
| Diesel oil | 28.40 | 23.83 |
| Slurry oil | 2.14 | 2.01 |
| Extracting aromatic hydrocarbons | 8.26 | 8.23 |
| Coke | 8.16 | 8.37 |
| Oxygenatedchemicals | 0.33 | |
| Add up to | 100.00 | 100.00 |
| Total liquid yield, heavy % | 78.76 | 78.24 |
| Gasoline octane rating | ||
| RON | 95.8 | 92.6 |
| MON | 83.7 | 81.0 |
Claims (10)
1. produce the method for light-weight fuel oil and propylene from inferior feedstock oil for one kind, it is characterized in that the method comprises the following steps:
(1), the first reaction zone that the inferior feedstock oil of preheating enters catalytic conversion reactor contacts the cracking reaction of generation macromole with the regeneration catalyzing conversion catalyst of heat, the condition of the first reaction zone comprises that temperature of reaction is 510 ℃～650 ℃, reaction times is 0.05 second～1.0 seconds, the weight ratio of catalyzer and stock oil is 3～15: 1, the weight ratio of water vapor and stock oil is 0.03～0.3: 1, pressure is 130kPa～450kPa, the oil gas that generates and used catalyst or with the second reaction zone that enters catalytic conversion reactor after the lightweight material oil that injects and/or cold shock medium mix, it is 420 ℃～550 ℃ in temperature of reaction, reaction times is to carry out cracking reaction under 1.5 seconds～20 seconds the condition, hydrogen transfer reactions and isomerization reaction, after reaction product and the reaction with the reclaimable catalyst of charcoal after gas solid separation, reaction product enters separation system and is separated into dry gas, propylene, propane, the C4 hydrocarbon, gasoline, diesel oil and catalytic wax oil, reclaimable catalyst is transported to revivifier and carries out coke burning regeneration behind the water vapor stripping, the regenerated catalyst Returning reactor of heat recycles;
(2), described catalytic wax oil enters aromatic extraction unit, separate obtaining extracting oil out and raffinating oil;
(3), described the first reaction zone that is circulated to step (1) catalytic conversion reactor of raffinating oil obtains purpose product propylene and gasoline or/and other catalytic convention design is further reacted.
2. according to the method for claim 1, it is characterized in that described inferior feedstock oil is heavy petroleum hydrocarbon and/or other mineral oil, wherein heavy petroleum hydrocarbon is selected from one or more the mixture of arbitrary proportion in vacuum residuum, inferior long residuum, hydrogenated residue inferior, coker gas oil, deasphalted oil, crude oil with high acid value, the high metal crude oil; Other mineral oil is one or more in liquefied coal coil, tar sand oil, the shale oil.
3. according to the method for claim 1 or 2, it is characterized in that described inferior raw material oil properties satisfies a kind of in the following index at least: density is 900～1000 kg/m 3, carbon residue is 4～15 heavy %, and metal content is 15～600ppm, and acid number is 0.5～20mgKOH/g.
4. according to the method for claim 1, it is characterized in that one or more in liquefied gas, gasoline, diesel oil of described lightweight material grease separation.
5. according to the method for claim 1, it is characterized in that described cold shock medium is one or more the mixture of arbitrary proportion in half regenerated catalyst, reclaimable catalyst and the live catalyst of the regenerated catalyst that is selected from cold shock agent, cooling, cooling, wherein the cold shock agent is one or more the mixture of arbitrary proportion that is selected from liquefied gas, raw gasline, stable gasoline, diesel oil or the water; The regenerated catalyst of cooling and half regenerated catalyst of cooling are that reclaimable catalyst cools off after two-stage regeneration and one section regeneration respectively and obtains.
6. according to the method for claim 1, it is characterized in that described catalytic converting catalyst comprises zeolite, inorganic oxide and optional clay, each component accounts for respectively total catalyst weight: the heavy % of zeolite 1 heavy %-50, the heavy % of inorganic oxide 5 heavy %-99, the heavy % of clay 0 heavy %-70, its mesolite is as active ingredient, be mesopore zeolite and/or optional large pore zeolite, mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, and large pore zeolite is selected from by Rare Earth Y, rare earth hydrogen Y, the super steady Y that different methods obtains, the mixture of one or more in this group zeolite that high silicon Y consists of.
7. according to the method for claim 1, it is characterized in that the condition of the first reaction zone: temperature of reaction is that 520 ℃～600 ℃, reaction times are that the weight ratio of 0.1 second～0.5 second, catalyzer and stock oil is 4～12: 1, the weight ratio of water vapor and stock oil is 0.05～0.2: 1, pressure is 130kPa～450kPa.
8. according to the method for claim 1, it is characterized in that the condition of second reaction zone: temperature of reaction is that 460 ℃～530 ℃, reaction times are 2 seconds～10 seconds.
9. according to the method for claim 1, it is characterized in that at least aly in described propane, C4 hydrocarbon, the diesel oil entering described second reaction zone as lightweight material oil.
10. according to the method for claim 1, the solvent that it is characterized in that described Aromatics Extractive Project is selected from furfural, methyl-sulphoxide, dimethyl formamide, monoethanolamine, ethylene glycol, 1, in the 2-propylene glycol one or more, temperature is 40～120 ℃, and the volume ratio of catalytic wax oil and solvent is 0.5～5.0: 1.
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| CN 200810225606 CN101724430B (en) | 2008-10-31 | 2008-10-31 | Method for preparing light-weight fuel oil and propylene from inferior raw oil |
| KR1020107018801A KR101606496B1 (en) | 2008-03-13 | 2009-03-13 | Method for obtaining light fuel from inferior feedstock |
| JP2010550019A JP5879038B2 (en) | 2008-03-13 | 2009-03-13 | Method for obtaining light fuel from low quality feedstock |
| US12/921,436 US8597500B2 (en) | 2008-03-13 | 2009-03-13 | Process for converting inferior feedstock to high quality fuel oil |
| PCT/CN2009/000272 WO2009111953A1 (en) | 2008-03-13 | 2009-03-13 | Method for obtaining light fuel from inferior feedstock |
| RU2010133616/04A RU2497933C2 (en) | 2008-03-13 | 2009-03-13 | Method for conversion of low-grade raw feedstock to high-quality oil fuel |
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| CN101899320B (en) * | 2009-05-27 | 2013-09-25 | 中国石油化工股份有限公司 | Catalytic conversion method for producing high cetane number light diesel oil |
| CN102371191B (en) * | 2010-08-26 | 2015-09-23 | 中国石油化工股份有限公司 | Improve catalytic cracking catalyst optionally processing method |
| RU2563637C2 (en) | 2010-09-27 | 2015-09-20 | Чайна Петролеум Энд Кемикал Корпорейшн | Method of catalytic conversion for improvement of composition of target product |
| CN102417828B (en) * | 2010-09-27 | 2014-08-20 | 中国石油化工股份有限公司 | Catalytic conversion method for improving product distribution |
| CN102796556B (en) * | 2011-05-26 | 2015-08-26 | 中国石油化工股份有限公司 | A kind of catalysis conversion method of petroleum hydrocarbon |
| CN102796557B (en) * | 2011-05-26 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of effective catalysis conversion method of petroleum hydrocarbon |
| CN102796558B (en) * | 2011-05-26 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of Catalytic conversion method of petroleum hydrocarbon |
| CN102911734B (en) * | 2011-08-04 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of high-sulfur wax oil |
| CN102911732B (en) * | 2011-08-04 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of high-sulfur wax oil |
| CN103059994B (en) * | 2011-10-20 | 2015-02-25 | 中国石油化工股份有限公司 | Catalytic conversion method of petroleum hydrocarbon |
| CN103059991B (en) * | 2011-10-20 | 2015-02-25 | 中国石油化工股份有限公司 | High-efficiency catalytic conversion method of petroleum hydrocarbon |
| CN103059992B (en) * | 2011-10-20 | 2015-02-25 | 中国石油化工股份有限公司 | Effective catalytic conversion method of petroleum hydrocarbon |
| CN103627426A (en) * | 2012-08-23 | 2014-03-12 | 中国石油化工股份有限公司 | Method for improving gasoline yield of catalytic cracking technology and device thereof |
| CN106590740B (en) * | 2015-10-15 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of inferior raw material oil treatment process |
| CN107267211B (en) * | 2016-04-06 | 2019-03-22 | 中国石油化工股份有限公司 | A kind of processing method and system of inferior feedstock oil |
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