CN102371190A - Treatment method for improving selectivity of catalytic cracking catalyst - Google Patents
Treatment method for improving selectivity of catalytic cracking catalyst Download PDFInfo
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- CN102371190A CN102371190A CN201010263278XA CN201010263278A CN102371190A CN 102371190 A CN102371190 A CN 102371190A CN 201010263278X A CN201010263278X A CN 201010263278XA CN 201010263278 A CN201010263278 A CN 201010263278A CN 102371190 A CN102371190 A CN 102371190A
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Abstract
The invention relates to a treatment method for improving the selectivity of a catalytic cracking catalyst. The method comprises the following steps of: feeding the fresh catalyst in a fluidized bed, preferably a dense-phase fluidized bed; introducing fuel and a gas containing oxygen into the fluidized bed, so that the fuel combusts to release heat; and introducing water vapor to be in contact with the catalyst, and carrying out aging under a certain hydrothermal environment. According to the method disclosed by the invention, the activity and selectivity distribution of the catalyst in a catalytic cracking device is more uniform, and the selectivity of the catalytic cracking catalyst is remarkably improved, therefore the gas yield and the coke yield are remarkably reduced, the water vapor is fully utilized, and the energy consumption of the device is reduced.
Description
Technical field
The present invention relates to the processing method of catalytic cracking field inner catalyst, more particularly, is a kind of optionally processing method of catalytic cracking catalyst of improving.
Background technology
The y-type zeolite that early 1960s uses the earliest is Rare Earth Y (REY) zeolite through rare earth exchanged.REY zeolite silica alumina ratio is less than 5, and content of rare earth is with RE
2O
3Meter is not less than 17 heavy % (accounting for zeolite), and acid site density is high, and the hydrogen migration performance is strong, and alkene and naphthene content are low in the gasoline, causes octane number to descend, and has to lead tetraethide as the additive that improves octane number.However, y-type zeolite is the main active component of heavy petroleum hydrocarbon fluid catalytic cracking (FCC) catalyst system therefor always.
U.S.'s cancellation leaded gasoline in 1975 has occurred replacing the Cracking catalyst of REY zeolite as active component with ultra steady Y (USY) zeolite.USY is a kind of high-silicon Y-Zeolite that the y-type zeolite framework dealumination is processed through the hydrothermal treatment consists method, and the silica alumina ratio of this zeolite generally between 5～10, does not contain or contain a small amount of rare earth.Because the framework si-al ratio of USY improves, acid site density reduces, its hydrogen migration performance weakens.Thereby the olefin(e) centent of gasoline increases, octane number improves.
Early 1980s ZSM-5 class is selected the type zeolite and is begun to be applied to the FCC catalyst, in order to improve the octane number of gasoline.The effect of ZSM-5 in FCC is actually optionally that octane number in the gasoline fraction is low straight chain hydrocarbon and is cracked into low-carbon alkene, and with part low-carbon alkene aromatisation, the octane number of gasoline is improved.Therefore, the application of ZSM-5 can cause the increase of alkene in the gasoline, arene content inevitably.High-silicon Y-Zeolite is mainly used in the coke and the gas yield that increase FCC gasoline and distillate productive rate and reduce the FCC process as the catalyst activity constituent element.
No matter be the REY zeolite, the still USY zeolite of various silica alumina ratios can't satisfy the requirement to FCC purpose product selectivity well with the catalyst of its preparation.When its when being added into industrial catalyticing cracking device, the catalyst initial activity is all more than 85, REY type zeolite catalyst initial activity is especially up to more than 90.Two kinds of zeolite catalysts are under high-intensity hydrothermal treatment consists, and catalyst activity constantly reduces, and REY type activety of zeolite catalyst is in the straight line reduction; And USY type activety of zeolite catalyst is along with the increase of ageing time, and the initial activity decay is fast, then reduces slow (referring to Fluid Catalytic Cracking Handbook:Design; Operation, and Troubleshooting of FCC Facilities, Reza Sadeghbeigi; 2nd edition, P92, Fig. 3～5).
Former oil quality shows that mainly oil density becomes big along with the continuous increase of oil extraction amount worse and worse, and viscosity uprises, and heavy metal, sulphur, nitrogen, colloid 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 processing method more and more to receive publicity; That is to say, from crude oil with poor quality, improve the yield of light oil as much as possible, this has brought great challenge for the process technology of traditional crude oil.In order to satisfy the growing low-carbon alkene industrial chemicals and the demand of motor petrol; PCT/CN2009/000272 discloses a kind of method of producing light-weight fuel oil and propylene from inferior feedstock oil; First and second reaction zone that inferior feedstock oil gets into catalytic conversion reactor successively contacts with catalytic converting catalyst primary first-order equation, secondary response takes place respectively; Product and reclaimable catalyst after gas solid separation, reclaimable catalyst successively through stripping, burn again after Returning reactor recycle; Product obtains propylene, gasoline, catalytic wax oil and other product through separation, and wherein said catalytic wax oil gets into aromatic extraction unit, separates to obtain extracting oil out and raffinating oil; Said 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.Inferior feedstock oil is after relaxing catalyzed conversion in this method, and resulting catalytic wax oil is extracted out in the oil and is rich in double ring arene through the aromatic hydrocarbons extracting, is good industrial chemicals; Raffinate oil and be rich in alkane and cycloalkane, be fit to very much carry out catalyzed conversion, realized that petroleum resources efficiently utilize.This method can reduce dry gas yied and coke yield significantly.The catalyst that this method adopted is to be main with catalyst to the purpose product selectivity.
Catalyst in the industrial catalyticing cracking device exists continuous wearing and tearing and runs off in operation process; To add in order keeping reacting required equilibrium catalyst activity and often to draw off the partial equilibrium catalyst; (at present general fresh catalyst activity is more than 85 for compelled simultaneously fresh makeup catalyst; Dry gas and coke selectivity extreme difference), so just exist the reasonable replacement speed of fresh catalyst to the system balancing catalyst inventory.Therefore, equilibrium catalyst is that fresh catalyst constantly adds and the system balancing catalyst runs the coefficient result of damage (comprising that the people is for unloading agent) continuously.The method of present catalytic cracking unit fresh makeup catalyst; Usually take following way: the fresh catalyst that from the fresh catalyst storage tank, takes; Get into manually or the auto feed appearance, through weigh, discharging after the blowing air fluidisation, in the regenerator with catalyst transport to catalytic cracking unit.
The hydrothermal deactivation of catalyst is that an average life span is 30～100 days a slow process; In inactivation; The operating condition of the activity of fresh catalyst, the tenor of feedstock oil and other character, device, the turnover rate of catalyst and the rate that draws off all are difficult to constant; Simultaneously; The fresh catalyst of individual particle has just lost its physics and chemical property in the moment that gets into complete mixed flow regenerator, and these problems bring difficulty for the age distribution and the activity distribution thereof of the catalyst in the accurate prediction industrial catalyticing cracking device.In industrial catalyticing cracking device, directly take the equilibrium catalyst sample to measure active or other character of equilibrium catalyst; Perhaps come calculated equilibrium activity of such catalysts or other character based on the Mathematical Modeling of simplifying, resulting equilibrium catalyst activity or other character are the mean value of average activity or other character.These numerical value are production operations and optimization products distribution and product property key parameter of instructing device; But produce a serious problem simultaneously, ignored the influence difference of interior all the individual particle catalyst of industrial catalyticing cracking device exactly products distribution and product property.CN1382528A discloses a kind of catalyst circulation and has polluted and aging method, and fresh catalyst is after this method is handled, and its each item physico-chemical property all approaches industrial poising agent.This method is primarily aimed at the handled catalyst in laboratory and industrial equilibrium catalyst difference designs, but can not improve the activity difference between the industrial equilibrium catalyst.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of optionally processing method of catalytic cracking catalyst of improving.
Thereby research shows the individual particle catalyst and has different cracking activities and selectivity because of the time of staying in industrial catalyticing cracking device is different.Most of catalyst ages are longer in the industrial catalyticing cracking device; Less to the activity contribution; After device moved 100 days, the catalyst that is added had half still to be deposited in the system approximately, but the contribution of activity is had only 5%; And the life-span has only 25 days catalyst amounts only to account for 1/6 of system's total amount, but the activity contribution of whole system is accounted for 2/3.Activity of such catalysts in the industrial catalyticing cracking device is approximately the function of regeneration temperature and steam partial pressure, and water vapour makes the catalysqt deactivation process exist " self-balancing " process, i.e. its inactivation influence weakens with the prolongation of ageing time.Simultaneously, result of study shows that catalyst is converted to equilibrium catalyst (lower micro-activity) from fresh catalyst (higher micro-activity), and dry gas and coke selectivity improve rapidly, until reaching balance.Therefore, improve the catalytic cracking selectivity best approach and will have higher optionally catalyst exactly and join in the industrial catalyticing cracking device, rather than the fresh catalyst that will have a greater activity directly joins in the industrial catalyticing cracking device.
In first aspect, a kind of optionally processing method of catalytic cracking catalyst of improving provided by the invention, this method comprises the following steps:
(1), with the fresh catalyst fluid bed of packing into, preferred dense-phase fluidized bed;
(2), fuel and oxygenous gas are introduced fluid bed, and make fuel that the burning release heat take place;
(3), feed water vapour and contact with catalyst, under certain thermal and hydric environment, wear out.
Technical scheme of the present invention for example is such practical implementation:
Fresh catalyst is packed in the preferred dense-phase fluidized bed of fluid bed, feed fuel and oxygenous gas in the bottom of fluid bed, catalyst is realized fluidisation under the effect of said gas; And make fuel that the burning release heat take place, and water vapour or aqueous water are injected in the bottom of fluid bed in meanwhile probable back, and catalyst is realized aging at water vapour; Aging temperature is 500 ℃～850 ℃; Preferred 650 ℃～790 ℃, the apparent linear speed of fluid bed is 0.1 meter per second～0.6 meter per second, is preferably 0.15 second～0.5 meter per second; Aging after 1 hour～720 hours preferred 5 hours～360 hours; Obtain the requirement of aging catalyst, join industrial catalyticing cracking device, preferably join the regenerator of industrial catalyticing cracking device by industrial catalyticing cracking device.
It is pointed out that in this article regenerator is regarded as the part of industrial catalyticing cracking device.
Said fuel is mainly made a general reference the material that contains C element and/or H element, comprises in fuel gas and the fuel wet goods one or more.
Said fuel gas mainly refers to fuel gas, comprises or is selected from the detailed hydrocarbons such as carbon monoxide, hydrogen, dry gas, liquefied gas, synthesis gas, natural gas, biogas, methane, ethane one or more.The gas that preferably contains carbon monoxide, more preferably carbon monoxide and hydrogen, wherein the mist of carbon monoxide and hydrogen can be produced from coke on the spent catalytic cracking catalyst, also can install from other.
Said fuel oil refers to that mainly flammable liquid is selected from one or more in gasoline, naphtha, diesel oil, heavy oil, crude oil, the synthetic wet goods.
It is 0.01%～99.9% that said water vapour accounts for fluid bed gaseous phase volume mark, preferred 15%～60%.
Said fluid bed aging temperature control method is following: directly fire fuel gas firing mode, or spray fuel oil combustion mode, or make fluidized-bed temperature surpass fuel gas or/and ignition temperature is introduced fuel gas then or/and fuel oil with other heat exchange means earlier.
Described catalyst comprises zeolite, inorganic oxide and optional clay, and each component accounts for total catalyst weight respectively: the heavy % in zeolite 1 heavy %～50, the heavy % in inorganic oxide 5 heavy %～99, the heavy % in clay 0 heavy %～70.Its mesolite is selected from mesopore zeolite and/or large pore zeolite as active component.Mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, also can carry out modification with transition metals such as nonmetalloid such as phosphorus and/or iron, cobalt, nickel to above-mentioned mesopore zeolite, and 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, and 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 ultra steady Y that is obtained by Rare Earth Y (REY), rare earth hydrogen Y (REHY), distinct methods, high silicon Y constitute.
Inorganic oxide is selected from silica (SiO as bonding agent
2) and/or alundum (Al (Al
2O
3).
Clay is selected from kaolin and/or halloysite as matrix (being carrier).
Gas after the aging step can be used as in stripped vapor, anti-scorch steam, atomizing steam, the lifting steam one or more and gets into stripper, settler, raw material nozzles and/or pre lift zone in the catalytic cracking unit respectively, also can be used for other purposes like loosening steam etc.
Gas after the aging step can be used for heat exchange.
In second aspect, the invention provides the purposes of catalyst in catalytic cracking process according to first aspect, wherein said catalyst is added in the industrial catalyticing cracking device (preferred regenerator) and be used to carry out catalytic cracking process.Those skilled in the art will appreciate that obviously the various characteristics of above-mentioned first aspect all are applicable to said second aspect.
The present invention compared with prior art has following technique effect:
1, activity of such catalysts and the selectivity more even distribution in the catalytic cracking unit.
2, improve the selectivity of catalytic cracking catalyst significantly, thereby dry gas yied and coke yield reduce significantly.
Only if indicate separately, all technology used herein have the implication identical with those skilled in the art's general understanding with scientific terminology.Although in practice of the present invention or test, can use and those similar or be equal to method and materials as herein described, hereinafter has still been described suitable method and material.Under the situation of conflict, be as the criterion with patent specification (comprising definition).In addition, these materials, method and embodiment only are exemplary and nonrestrictive.
Term used herein " comprises " and is meant and can adds other step and the composition that does not influence final result.This term comprise term " by ... form " with " basically by ... composition ".
Term " method " or " technology " are meant mode, means, technology and the program that is used to realize appointed task; Include but not limited to chemistry and chemical field practitioner those modes, means, technology and program known or that they are gone out by known way, means, technology and program development easily.
In the disclosure, various aspects of the present invention can be represented with range format.The description that it should be understood that range format is merely convenient and concise and to the point purpose use, should not be regarded as the rigidity restriction to the scope of the invention.Correspondingly, the description of a scope should be regarded as and specifically disclose all possible subrange and the numerical value one by one in this scope.For example, the description of the scope as 1 to 6 should be regarded as the subrange that specifically discloses as 1 to 3,1 to 4,1 to 5,2 to 4,2 to 6,3 to 6 and so on, and the numerical value one by one in this scope, and for example 1,2,3,4,5 and 6.Regardless of the fabric width of this scope, this all is suitable for.
As long as point out number range in this article, any numerical value (mark or integer) of enumerating in the scope shown in being intended to comprise.Phrase " " numerical value shown in first " and " numerical value shown in second " between " and " from " the interchangeable in this article use of numerical value shown in first " extremely " numerical value shown in second and be intended to comprise this numerical value and all marks and integer between them shown in first and second.
Description of drawings
With reference to accompanying drawing the present invention is only described for example among this paper.Now at length especially with reference to accompanying drawing; Stress; Shown in details only as embodiment with only be used to illustrate the preferred embodiments of the invention, and appear for the description that it is believed that the most useful and easy understanding that principle of the present invention and notion aspect are provided.In this respect, except that basic comprehension the present invention is necessary, do not attempt more detail CONSTRUCTED SPECIFICATION of the present invention, this description of connection with figures makes those skilled in the art how understand fully practical implementation several kinds of forms of the present invention.
Fig. 1 is the basic procedure sketch map of the catalysis conversion method relevant with the present invention, and Fig. 2 is the optionally process flow diagram of processing method of catalytic cracking catalyst that improves provided by the invention.
The specific embodiment
Further specify method provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention does not receive any restriction.
Fig. 1 is the basic procedure sketch map of the catalysis conversion method relevant with the present invention.
Promoting medium is in advance got into by riser reactor 2 bottoms through pipeline 1; From the regenerated catalyst of pipeline 16 in the castering action lower edge riser that the promotes medium in advance accelerated motion that makes progress; Part material oil through pipeline 3 with 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 takes place in feedstock oil on the catalyst of heat, and upwards accelerated motion.Part freshening feedstock oil through pipeline 5 with middle and upper part from the atomizing steam injecting lift pipe 2 reaction zone I of pipeline 6; Mix with the existing logistics of riser reactor; Cracking reaction takes place in feedstock oil on the lower catalyst that contains certain charcoal; And the accelerated motion entering reaction zone II continuation reaction that makes progress, the cyclone separator that the product oil gas of generation and the reclaimable catalyst of inactivation get in the settlers 8 through pipeline 7, the realization reclaimable catalyst separates with product oil gas; Product oil gas gets into collection chamber 9, and catalyst fines returns settler by dipleg.Reclaimable catalyst flows to stripping section 10 in the settler, contacts with water vapour from pipeline 11.The product oil gas that stripping goes out from reclaimable catalyst gets into collection chamber 9 behind cyclone separator.Reclaimable catalyst behind the stripping gets into regenerator 13 through inclined tube 12, and main air gets into regenerator through pipeline 14, and the coke on the burning-off reclaimable catalyst makes the reclaimable catalyst regeneration of inactivation, and flue gas gets into the cigarette machine through pipeline 15.Catalyst after the regeneration gets into riser through inclined tube 16.
Product oil gas in the collection chamber 9 gets into follow-up piece-rate system 18 through main oil gas piping 17, separates the dry gas that obtains and draws through pipeline 19; Separating the liquefied gas that obtains draws through pipeline 20; Separating the gasoline that obtains draws through pipeline 21; Separating the diesel oil that obtains draws through pipeline 22; Separating the slurry oil that obtains draws through pipeline 23.Wherein each cut boiling range is regulated according to refinery's actual needs.
Fig. 2 is the optionally a kind of process flow diagram of processing method of catalytic cracking catalyst that improves provided by the invention.But the position of fresh catalyst ager is not confined to the regenerator next door, and the catalyst after wearing out does not limit to be got back in the regenerator.
Can fresh catalyst ager of design be dense-phase fluidized bed 9 on regenerator 2 next doors; Fresh catalytic cracking catalyst is packed in the dense-phase fluidized bed 9; Water vapour mixes in pipeline 8 with fuel from pipeline 6 through pipeline 7; Mixed gas is got into through distribution grid 12 by dense-phase fluidized bed 9 bottoms, and air gets into dense-phase fluidized bed 9, fuel and oxygen generation oxidation reaction release heat through pipeline 11 through distribution grid 12; Fresh catalyst generation aging reaction in the dense-phase fluidized bed 9, the gas after wearing out is sent to heat exchange through pipeline 10.Catalyst after aging is by the requirement of industrial catalyticing cracking device; In pipeline 5 joins the regenerator 2 of industrial catalyticing cracking device; Main air gets into 2 pairs of catalyst of regenerator through pipeline 1 and regenerates; Flue gas after the regeneration carries out gas solid separation through cyclone separator 3, and the flue gas after the separation leaves regenerator through pipeline 4.
Following embodiment will further specify the present invention, but therefore not limit the present invention.Employed feedstock oil is the mixture of 60 heavy % vacuum gas oil (VGO)s (VGO) and 40 heavy % decompression residuum (VR) in embodiment and the Comparative Examples, and its character is listed in table 1.The trade names of catalyst system therefor are CGP-1Z in embodiment and the Comparative Examples, produce for Sinopec catalyst branch company Shandong catalyst plant, and its character is listed in table 2.
This embodiment makes an experiment according to the flow process of Fig. 1 and 2; (this fresh catalyst activity is 89 to fresh catalyst CGP-1Z; In temperature is that self regulation time is 40h under 800 ℃ and the 100% water vapour condition, and equilibrium activity is 58) hydrogen content is 51.7% in 700 ℃, 30% water vapour, fuel gas, carbon monoxide content is 23.8%; After apparent linear speed 0.23 meter per second, ageing time wore out in 21 hours, the initial activity of gained catalyst was 71.Catalyst make-up with this after aging, makes an experiment on the middle-scale device of riser reactor with the raw material of feedstock oil A as catalytic cracking to regenerator; Feedstock oil gets into the riser reactor bottom; Contact with catalyst CGP-1Z and catalytic cracking reaction takes place, at reaction zone I, reaction temperature is 528 ℃; The weight ratio of catalyst and feedstock oil is 6.5, and the weight ratio of water vapour and feedstock oil is 0.05; At reaction zone II, the weight ratio of 513 ℃ of water vapours of reaction temperature and feedstock oil is 0.05.Operating condition and product distribute and list in table 3.
Comparative Examples 1
This Comparative Examples is that the flow process according to Fig. 1 makes an experiment, and fresh catalyst CGP-1Z just directly adds to regenerator without aging, and the feedstock oil of employing is identical with embodiment 1.Operating condition and product distribute and list in table 3.
Can find out that from table 3 with respect to Comparative Examples 1, the dry gas yied of embodiment 1 and coke yield reduce by 0.34 percentage point and 1.15 percentage points respectively, total liquid yield (liquefied gas yield+gasoline yield+diesel yield) has increased by 1.38 percentage points.
Table 1
| Feedstock oil is formed | 60％VGO+40％VR |
| The feedstock oil code name | A |
| Density (20 ℃), kilogram/rice 3 | 930.0 |
| Kinematic viscosity (100 ℃), millimeter 2/ second | 16.36 |
| Carbon residue, heavy % | 4.3 |
| Condensation point, |
22 |
| Acid number, mgKOH/g | 0.25 |
| Nitrogen, heavy % | 0.18 |
| Sulphur, heavy % | 1.20 |
| Carbon, heavy % | 86.59 |
| Hydrogen, heavy % | 12.58 |
| Tenor, ppm | |
| Nickel | 4.7 |
| Vanadium | 5.0 |
| Iron | 25.3 |
| Copper | ＜0.1 |
| Sodium | 1.8 |
| Boiling range, ℃ | |
| Initial boiling point | 285 |
| 10％ | 393 |
| 30％ | 470 |
| 50％ | 516 |
| 70％ | 548 |
| 90％ | 581 |
| The end point of distillation | / |
Table 2
| The catalyst numbering | A |
| Bulk density, kg/m 3 | 0.77 |
| Pore volume, milliliter/gram | 0.2 |
| Specific area, rice 2/ gram | 110 |
| Abrasion index is when weighing % -1 | 1.1 |
| Size consist, heavy % | |
| The 0-40 |
15 |
| The 40-80 micron | 59 |
| ＞80 microns | 26 |
| Fresh catalyst is active | 89 |
| Self regulation time, hour | 40 |
| Equilibrium activity | 58 |
Table 3
Recognize, for clarity sake be described in some aspect of the present invention and characteristic in the embodiment separately and also can in single embodiment, unite and provide.On the contrary, for the purpose of concise and to the point, in single embodiment, describe of the present invention various aspect also can separately provide or provide with characteristic with any suitable sub-compound mode.
All publications, patent and the patent application of mentioning in this specification all quoted through this in full and incorporated this specification into, pointed out specially and one by one to quote through this just as each publication, patent or patent application and incorporates this paper into.
Although got in touch specific embodiments and embodiment has been described the present invention, be apparent that those skilled in the art can find out many replacement schemes, modification and change.Correspondingly, be intended to contain spirit and interior all such replacement schemes, modification and the change of wide region that drops on accompanying claims.
Claims (11)
1. one kind is improved optionally processing method of catalytic cracking catalyst, it is characterized in that this method comprises the following steps:
(1), with the fresh catalyst fluid bed of packing into;
(2), fuel and oxygenous gas are introduced fluid bed, and make fuel that the burning release heat take place;
(3), feed water vapour and contact with catalyst, under certain thermal and hydric environment, wear out.
2. according to the method for claim 1; It is characterized in that described fresh catalyst comprises zeolite, inorganic oxide and optional clay; Each component accounts for total catalyst weight respectively: the heavy % in zeolite 1 heavy %～50, the heavy % in inorganic oxide 5 heavy %～99, the heavy % in clay 0 heavy %～70, its mesolite is selected from mesopore zeolite and/or large pore zeolite.
3. according to the method for claim 1, it is characterized in that aging temperature is 500 ℃～850 ℃, the apparent linear speed of dense-phase fluidized bed is 0.1 meter per second～0.6 meter per second, and ageing time is 1 hour～720 hours.
4. according to the method for claim 3, it is characterized in that aging temperature is that 650 ℃～790 ℃, the apparent linear speed of dense-phase fluidized bed are 0.15 second～0.5 meter per second, ageing time is 5 hours～360 hours.
5. according to the method for claim 1, it is characterized in that said fuel refers to contain the material of C element and/or H element, is selected from fuel gas or/and fuel oil.
6. according to the method for claim 5, it is characterized in that said fuel gas comprises or is selected from carbon monoxide, hydrogen, dry gas, liquefied gas, synthesis gas, natural gas, biogas, methane, the ethane one or more.
7. according to the method for claim 5, it is characterized in that said fuel oil is selected from one or more in gasoline, naphtha, diesel oil, heavy oil, crude oil, the artificial oil.
8. according to the method for claim 1; It is characterized in that said fluid bed aging temperature control method is following: direct fire fuel gas firing mode; Or spray fuel oil combustion mode; Or make fluidized-bed temperature surpass fuel gas or/and ignition temperature is introduced fuel gas then or/and fuel oil with other heat exchange means earlier.
9. according to the method for claim 1, it is characterized in that it is 0.01%～99.9% that said water vapour accounts for fluid bed gaseous phase volume mark.
10. according to the method for claim 9, it is characterized in that it is 15%～60% that said water vapour accounts for fluid bed gaseous phase volume mark.
11., it is characterized in that said fluid bed is a dense-phase fluidized bed according to the method for claim 1.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105631107A (en) * | 2015-12-23 | 2016-06-01 | 浙江中控软件技术有限公司 | Prediction method and apparatus for fluidized catalytic cracking reaction |
| CN108654702A (en) * | 2018-03-29 | 2018-10-16 | 南京大学连云港高新技术研究院 | A kind of catalyst of inferior heavy oil cracking desulfurization visbreaking, preparation method and applications |
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| CN1382528A (en) * | 2001-04-28 | 2002-12-04 | 中国石油化工股份有限公司 | Cyclic polluting and ageing process for catalyst |
| CN101209391A (en) * | 2006-12-30 | 2008-07-02 | 中国石油化工股份有限公司 | Method for removing oxysulfide and/or nitrogen oxide from flue gas and hydrocarbon oil cracking method |
| CN101531924A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
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|---|---|---|---|---|
| CN1382528A (en) * | 2001-04-28 | 2002-12-04 | 中国石油化工股份有限公司 | Cyclic polluting and ageing process for catalyst |
| CN101209391A (en) * | 2006-12-30 | 2008-07-02 | 中国石油化工股份有限公司 | Method for removing oxysulfide and/or nitrogen oxide from flue gas and hydrocarbon oil cracking method |
| CN101531924A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105631107A (en) * | 2015-12-23 | 2016-06-01 | 浙江中控软件技术有限公司 | Prediction method and apparatus for fluidized catalytic cracking reaction |
| CN105631107B (en) * | 2015-12-23 | 2019-01-29 | 浙江中控软件技术有限公司 | A kind of prediction technique and device of fluid catalytic cracking reaction |
| CN108654702A (en) * | 2018-03-29 | 2018-10-16 | 南京大学连云港高新技术研究院 | A kind of catalyst of inferior heavy oil cracking desulfurization visbreaking, preparation method and applications |
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