CN102371190B - One improves the selective processing method of catalytic cracking catalyst - Google Patents
One improves the selective processing method of catalytic cracking catalyst Download PDFInfo
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Abstract
One improves the selective processing method of catalytic cracking catalyst, fresh catalyst is loaded fluid bed, preferably dense-phase fluidized bed, fuel and oxygenous gas are introduced fluid bed, and make fuel generation combustion heat release amount, it is passed through water vapour and contacts with catalyst, carrying out aging under certain thermal and hydric environment.The method makes the activity and selectivity of catalytic cracking unit inner catalyst be distributed more uniform, it will be apparent that improves the selectivity of catalytic cracking catalyst, thus reduces dry gas yied and coke yield significantly, takes full advantage of water vapour, thus reduce the energy consumption of device.
Description
Technical field
The present invention relates to the processing method of catalytic cracking field inner catalyst, more specifically, be that one improves the selective processing method of catalytic cracking catalyst.
Background technology
The y-type zeolite that early 1960s uses the earliest is Rare Earth Y (REY) zeolite through rare earth exchanged.REY Zeolite is less than 5, and content of rare earth is with RE2O3Meter is not less than 17 weights % (accounting for zeolite), and acid site density is high, and hydrogen migration performance is strong, and in gasoline, alkene and naphthene content are low, cause octane number to decline, and have to using lead tetraethyl as carrying high-octane additive.However, y-type zeolite is always the main active component of heavy petroleum hydrocarbon fluid catalytic cracking (FCC) used catalyst.
Within 1975, the U.S. cancels leaded gasoline, occurs in that and replaces the REY zeolite Cracking catalyst as active component using super steady Y (USY) zeolite.USY is a kind of high-silicon Y-Zeolite making y-type zeolite framework dealumination by hydrothermal treatment consists method and making, the silica alumina ratio of this zeolite typically between 5～10, without or containing a small amount of rare earth.Owing to framework si-al ratio raising, the acid site density of USY reduce, its hydrogen migration impaired performance.Thus, the olefin(e) centent of gasoline increases, octane number improves.
Early 1980s ZSM-5 class is selected type zeolite and is started to be applied to FCC catalyst, in order to improve the octane number of gasoline.Straight chain hydrocarbon low for octane number in gasoline fraction is actually optionally cracked into low-carbon alkene by ZSM-5 effect in FCC, and by part low-carbon alkene aromatisation, makes the octane number of gasoline be improved.Therefore, the application of ZSM-5 inevitably causes the increase of alkene in gasoline, arene content.High-silicon Y-Zeolite, as catalyst activity constituent element, is mainly used in increasing FCC gasoline and distillate productivity and reducing coke and the gas yield of FCC process.
Either REY zeolite, or the USY zeolite of various silica alumina ratio, can't meet the requirement of product selectivity to FCC mesh well with its catalyst prepared.When it is when being added into industrial catalyticing cracking device, catalyst initial activity is all more than 85, and REY type zeolite catalyst initial activity is more up to more than 90.Two kinds of zeolite catalysts are under the hydrothermal treatment consists of high intensity, catalyst activity constantly reduces, and REY type activety of zeolite catalyst is in straight line reduction, and USY type activety of zeolite catalyst is along with the increase of ageing time, initial activity decay is fast, then reduce and (see FluidCatalyticCrackingHandbook:Design, Operation, andTroubleshootingofFCCFacilities slowly, RezaSadeghbeigi, 2ndedition, P92, Fig. 3～5).
Crude quality along with being continuously increased of oil extraction amount worse and worse, is mainly manifested in oil density and becomes big, and viscosity uprises, and heavy metal, sulfur, nitrogen, resin and asphalt content and acid number uprise.At present, crude oil with poor quality is the most increasing along with the shortage of petroleum resources with the price difference of high-quality crude, cheap crude oil with poor quality exploitation and processing method is caused increasingly to receive publicity, that is, improving the yield of light oil from crude oil with poor quality as much as possible, this brings huge challenge to the process technology of traditional crude oil.In order to meet growing low-carbon alkene industrial chemicals and the demand of motor petrol, PCT/CN2009/000272 discloses a kind of method producing light-weight fuel oil and propylene from inferior feedstock oil, inferior feedstock oil sequentially enters first and second reaction zone of catalytic conversion reactor and contacts with catalytic converting catalyst primary first-order equation, secondary response occur respectively, product and reclaimable catalyst after gas solid separation, reclaimable catalyst successively through stripping, burn again after Returning reactor recycle；Product is isolated to propylene, gasoline, catalytic wax oil and other products, and wherein said catalytic wax oil enters aromatic extraction unit, isolated tapped oil and raffinating oil；Described raffinating oil is recycled to the first reaction zone of catalytic conversion reactor and obtains purpose product propylene and gasoline or/and other catalytic convention design is reacted further.In the method, inferior feedstock oil is after relaxing catalyzed conversion, and obtained catalytic wax oil rich in double ring arene, is good industrial chemicals in Aromatics Extractive Project, tapped oil；Raffinate oil rich in alkane and cycloalkane, be especially suitable for carrying out catalyzed conversion, it is achieved that petroleum resources efficiently utilize.The method can be greatly reduced dry gas yied and coke yield.The catalyst that the method is used is based on the catalyst selectivity to purpose product.
Catalyst in industrial catalyticing cracking device also exists constantly abrasion in operation process and runs off, add and often draw off partial equilibrium catalyst to keep reacting required equilibrium catalyst activity, be forced fresh makeup catalyst (the most general fresh catalyst activity is more than 85 simultaneously, dry gas and coke selectivity extreme difference), thus there is the fresh catalyst reasonable replacement speed to system balancing catalyst inventory.Therefore, equilibrium catalyst is that fresh catalyst is continuously added and runs damage (including artificially unloading agent) coefficient result continuously with system balancing catalyst.The method of catalytic cracking unit fresh makeup catalyst at present, following way it is usually taken: the fresh catalyst taken from fresh catalyst storage tank, enter and manually or automatically feed instrument, be weighed, discharging after blowing air fluidisation, by the regenerator of catalyst transport to catalytic cracking unit.
The hydrothermal deactivation of catalyst be average life be the slow process of 30～100 days, in inactivation, the activity of fresh catalyst, the tenor of raw oil and other character, the operating condition of device, the turnover rate of catalyst and the rate that draws off all are difficult to constant, simultaneously, the fresh catalyst of individual particle just loses its physics and chemical property entering the moment being thoroughly mixed flowing regenerator, and these problems bring difficulty to age distribution and the activity distribution thereof of the catalyst in Accurate Prediction industrial catalyticing cracking device.Directly take equilibrium catalyst sample to measure activity or other character of equilibrium catalyst in industrial catalyticing cracking device, or come activity or other character of calculated equilibrium catalyst based on the mathematical model simplified, obtained equilibrium catalyst activity or other character are the meansigma methods of average activity or other character.These numerical value are the production operation of guiding device and optimized product distribution and product property key parameter, but produce a serious problem, it is simply that in have ignored industrial catalyticing cracking device, all individual particle catalyst affect difference to products distribution and product property simultaneously.CN1382528A discloses a kind of catalyst cyclic polluting and aging method, and after treatment by using the treatment method, its every physico-chemical property is all close to industry poising agent for fresh catalyst.The method designs mainly for the catalyst handled by laboratory and industry equilibrium catalyst difference, but can not improve the activity difference between industry equilibrium catalyst.
Summary of the invention
It is an object of the invention to provide one to improve the selective processing method of catalytic cracking catalyst on the basis of existing technology.
Research show individual particle catalyst because of in industrial catalyticing cracking device the time of staying difference thus there is different cracking activities and selectivity.In industrial catalyticing cracking device, most of catalyst ages are longer, less to activity contribution, when after plant running 100 days, the catalyst added there are about half and still retains in systems, but the contribution to activity only has 5%, and the catalyst amounts that the life-span only has 25 days only accounts for the 1/6 of system total amount, but the activity contribution to whole system accounts for 2/3.The activity of the catalyst in industrial catalyticing cracking device is approximately the function of regeneration temperature and steam partial pressure, and water vapour makes catalysqt deactivation process there is " self-balancing " process, i.e. its inactivation to weaken with the prolongation of ageing time.Meanwhile, result of study shows, catalyst is converted to equilibrium catalyst (relatively low micro-activity) from fresh catalyst (higher micro-activity), and dry gas and coke selectivity improve rapidly, until it reaches balance.Therefore, improving the catalytic cracking selectivity best approach is exactly to join in industrial catalyticing cracking device by having higher selective catalyst rather than be added directly in industrial catalyticing cracking device by the fresh catalyst with greater activity.
In first aspect, the one that the present invention provides improves the selective processing method of catalytic cracking catalyst, and the method comprises the following steps:
(1), fresh catalyst is loaded fluid bed, preferably dense-phase fluidized bed；
(2), fuel and oxygenous gas are introduced fluid bed, and make fuel generation combustion heat release amount；
(3), it is passed through water vapour and contacts with catalyst, carrying out aging under certain thermal and hydric environment.
Technical scheme is the most so embodied as:
Fresh catalyst is loaded in the preferred dense-phase fluidized bed of fluid bed, fuel and oxygenous gas it is passed through in the bottom of fluid bed, catalyst realizes fluidisation under the effect of described gas, and make fuel generation combustion heat release amount, inject water vapour or aqueous water in the bottom of fluid bed after the most probable, catalyst realizes aging at water vapour, aging temperature is 500 DEG C～850 DEG C, preferably 650 DEG C～790 DEG C, the apparent linear velocity of fluid bed is 0.1 meter per second～0.6 meter per second, preferably 0.15 second～0.5 meter per second, aging 1 hour～720 hours preferably 5 hours～after 360 hours, obtain aging catalyst by the requirement of industrial catalyticing cracking device, join industrial catalyticing cracking device, it is added preferably to the regenerator of industrial catalyticing cracking device.
It is pointed out that in this article, regenerator is considered a part for industrial catalyticing cracking device.
Described fuel mainly refers to the material containing C element and/or H element, including one or more in fuel gas and fuel oil etc..
Described fuel gas refers mainly to fuel gas, including or one or more in the detailed hydrocarbon such as carbon monoxide, hydrogen, dry gas, liquefied gas, synthesis gas, natural gas, biogas, methane, ethane.Preferably containing the gas of carbon monoxide, more preferably carbon monoxide and hydrogen, wherein the mixed gas of carbon monoxide and hydrogen can come from coke on spent catalytic cracking catalyst and produces, it is also possible to from other device.
Described fuel oil refers mainly to one or more in gasoline, Petroleum, diesel oil, heavy oil, crude oil, artificial oil etc. of flammable liquid.
It is 0.01%～99.9% that described water vapour accounts for fluid bed gaseous phase volume mark, preferably 15%～60%.
Described fluid bed aging temperature control method is as follows: can directly light fuel gas combustion system, or spray fuel oil combustion mode, or first makes fluidized-bed temperature exceed fuel gas by other heat exchange means or/and ignition temperature, then introduces fuel gas or/and fuel oil.
Described catalyst includes zeolite, inorganic oxide and optional clay, and each component accounts for total catalyst weight respectively: zeolite 1 weight %～50 weight %, inorganic oxide 5 weight %～99 weight %, clay 0 weight %～70 weigh %.Wherein zeolite is as active component, selected from mesopore zeolite and/or large pore zeolite.Mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, also the transition metals such as the nonmetalloids such as above-mentioned mesopore zeolite phosphorus and/or ferrum, cobalt, nickel can be modified, the description the most detailed about ZRP sees US5,232,675, the ZSM series zeolite mixture of one or more among the zeolite of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other similar structures, the description the most detailed about ZSM-5 sees US3,702,886.The mixture of one or more in this group zeolite that super steady Y, the high silicon Y that large pore zeolite selects free Rare Earth Y (REY), rare earth hydrogen Y (REHY), distinct methods to obtain is constituted.
Inorganic oxide is as bonding agent, selected from silicon dioxide (SiO2) and/or aluminium sesquioxide (Al2O3)。
Clay is as substrate (i.e. carrier), selected from Kaolin and/or halloysite.
Gas after Aging Step can respectively enter the stripper in catalytic cracking unit, settler, raw material nozzles and/or pre lift zone as one or more in stripped vapor, anti-scorch steam, atomizing steam, lifting steam it can also be used to other purposes is as loosened steam etc..
Gas after Aging Step can be used to heat exchange.
In second aspect, the invention provides the purposes in catalytic cracking process of the catalyst according to first aspect, be used for carrying out catalytic cracking process in wherein described catalyst being added industrial catalyticing cracking device (preferably regenerator).Those skilled in the art obviously will appreciate that the various features of above-mentioned first aspect are all applicable to described second aspect.
The present invention compared with prior art has a following technique effect:
1, the activity and selectivity distribution of the catalyst in catalytic cracking unit is more uniform.
2, improve the selectivity of catalytic cracking catalyst significantly, thus dry gas yied and coke yield reduce significantly.
Unless otherwise specified, all technology used herein and scientific terminology have with those skilled in the art be commonly understood by identical implication.Although or the method for equivalent similar with those described herein and material can be used in the practice or test of the present invention, but the most still describe suitable method and material.In the case of a conflict, it is as the criterion with patent specification (including definition).Additionally, these materials, method and embodiment are only illustrative and not restrictive.
Term used herein " includes " referring to add other step and the composition not affecting final result.This term include term " consist of " and " substantially by ... composition ".
Term " method " or " technique " refer to for realizing the mode of appointed task, means, technology and program, include but not limited to, chemistry and chemical field practitioner is known or they are easily gone out by known way, means, technology and program development those modes, means, technology and program.
In the disclosure, the various aspects of the present invention can represent with range format.It should be understood that the description of range format only uses for convenience of with brief purpose, be not construed as the rigidity to the scope of the invention and limit.Correspondingly, the description of a scope should be considered to specifically disclose all possible subrange and numerical value one by one within the range.Such as, as the description of 1 to 6 such scope should be considered to specifically disclose such as 1 to 3, the subrange of 1 to 4,1 to 5,2 to 4,2 to 6,3 to 6 etc, and numerical value one by one within the range, such as 1,2,3,4,5 and 6.Regardless of the fabric width of this scope, this is all suitable for.
As long as pointing out numerical range in this article, it is intended that any enumerate numerical value (mark or integer) in the range of shown in including.Phrase " " numerical value shown in first " and " numerical value shown in second " between " and " from " numerical value shown in numerical value " extremely " second shown in first is used interchangeably herein and is intended to include this numerical value shown in first and second and all marks between them and integer.
Accompanying drawing explanation
Only illustrate the description present invention herein in reference to accompanying drawing.Now in detail referring specifically to accompanying drawing, it is however emphasized that, shown in details be only used as embodiment and be only used for illustrating the preferred embodiments of the invention, and be to provide for it is believed that description the most useful and easy to understand presents in terms of the principle of the present invention and concept.In this respect, in addition to necessary to the basic comprehension present invention, being not intended to show in more detail the CONSTRUCTED SPECIFICATION of the present invention, how this description of connection with figures can be be embodied as several forms of the present invention if making those skilled in the art understand fully.
Fig. 1 is the basic procedure schematic diagram of the catalysis conversion method relevant with the present invention, the process flow diagram improving the selective processing method of catalytic cracking catalyst that Fig. 2 provides for the present invention.
Detailed description of the invention
Further illustrate method provided by the present invention below in conjunction with the accompanying drawings, but the present invention is not therefore subject to any restriction.
Fig. 1 is the basic procedure schematic diagram of the catalysis conversion method relevant with the present invention.
Pre-lift medium enters by bottom riser reactor 2 through pipeline 1, from the regenerated catalyst of pipeline 16 under the castering action of pre-lift medium along riser upwards accelerated motion, part material oil is through pipeline 3 bottom of injecting lift pipe 2 reaction zone I together with the atomizing steam from pipeline 4, logistics existing with riser reactor mixes, cracking reaction, and upwards accelerated motion is there is in raw oil on the catalyst of heat.Part freshening raw oil is through pipeline 5 middle and upper part of injecting lift pipe 2 reaction zone I together with the atomizing steam from pipeline 6, logistics existing with riser reactor mixes, cracking reaction is there is in raw oil on the relatively low catalyst containing certain charcoal, and upwards accelerated motion enters reaction zone II continuation reaction, the product oil gas generated and the reclaimable catalyst of the inactivation cyclone separator in pipeline 7 enters settler 8, realize reclaimable catalyst to separate with product oil gas, product oil gas enters collection chamber 9, and catalyst fines is returned settler by dipleg.In settler, reclaimable catalyst flows to stripping section 10, contacts with the water vapour from pipeline 11.The product oil gas being stripped off from reclaimable catalyst enters collection chamber 9 after cyclone separator.Reclaimable catalyst after stripping enters regenerator 13 through inclined tube 12, and main air enters regenerator, the coke on burning-off reclaimable catalyst through pipeline 14, makes the reclaimable catalyst of inactivation regenerate, and flue gas enters cigarette machine through pipeline 15.Catalyst after regeneration enters riser through inclined tube 16.
Product oil gas in collection chamber 9, through main oil gas piping 17, enters follow-up piece-rate system 18, and the dry gas of isolated is drawn through pipeline 19；The liquefied gas of isolated is drawn through pipeline 20；The gasoline of isolated is drawn through pipeline 21；The diesel oil of isolated is drawn through pipeline 22；The slurry oil of isolated is drawn through pipeline 23.The most each fraction boiling range is actually needed according to refinery and is adjusted.
A kind of process flow diagram improving the selective processing method of catalytic cracking catalyst that Fig. 2 provides for the present invention.But the position of the aging device of fresh catalyst is not limited in regenerator side, aging after catalyst do not limit to and return in regenerator.
An i.e. dense-phase fluidized bed 9 of the aging device of fresh catalyst can be designed on regenerator 2 side, fresh catalytic cracking catalyst is loaded in dense-phase fluidized bed 9, water vapour mixes with the fuel from pipeline 6 through pipeline 7 in pipeline 8, mixed gas is entered through distribution grid 12 by bottom dense-phase fluidized bed 9, air enters dense-phase fluidized bed 9 through pipeline 11 through distribution grid 12, fuel and oxygen generation oxidation reaction release heat, fresh catalyst generation aging reaction in dense-phase fluidized bed 9, aging after gas send 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 enters regenerator 2 through pipeline 1 and regenerates catalyst, flue gas after regeneration carries out gas solid separation through cyclone separator 3, and the flue gas after separation leaves regenerator through pipeline 4.
The present invention will be further described by the following examples, but not thereby limiting the invention.Raw oil used in embodiment and comparative example is 60 weights % vacuum gas oil (VGO) (VGO) and the mixture of 40 weights % decompression residuum (VR), and its character is listed in table 1.Product designation CGP-1Z of used catalyst in embodiment and comparative example, produces for Sinopec catalyst branch company Shandong catalyst plant, and its character is listed in table 2.
Embodiment 1
This embodiment is tested according to the flow process of Fig. 1 and 2, (this fresh catalyst activity is 89 to fresh catalyst CGP-1Z, under the conditions of temperature is 800 DEG C and 100% water vapour, self regulation time is 40h, equilibrium activity is 58) through 700 DEG C, 30% water vapour, hydrogen content is 51.7% in fuel gas, carbon monoxide content is 23.8%, after apparent linear velocity 0.23 meter per second, ageing time 21 hours are aging, the initial activity of gained catalyst is 71.By this catalyst make-up after aging to regenerator, using raw oil A as the raw material of catalytic cracking, the middle-scale device of riser reactor is tested, raw oil enters bottom riser reactor, contacting with catalyst CGP-1Z and catalytic cracking reaction occurs, at reaction zone I, reaction temperature is 528 DEG C, catalyst is 6.5 with the weight ratio of raw oil, and water vapour is 0.05 with the weight ratio of raw oil；At reaction zone II, 513 DEG C of water vapour of reaction temperature are 0.05 with the weight ratio of raw oil.Operating condition and product slates are listed in table 3.
Comparative example 1
This comparative example is to test according to the flow process of Fig. 1, and fresh catalyst CGP-1Z the most directly adds to regenerator without aging, and the raw oil of employing is same as in Example 1.Operating condition and product slates are listed in table 3.
From table 3 it can be seen that relative to comparative example 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) adds 1.38 percentage points.
Table 1
| Raw oil forms | 60%VGO+40%VR |
| Raw oil code name | A |
| Density (20 DEG C), kg/m3 | 930.0 |
| Kinematic viscosity (100 DEG C), millimeter2/ the second | 16.36 |
| Carbon residue, weight % | 4.3 |
| Condensation point, DEG C | 22 |
| Acid number, mgKOH/g | 0.25 |
| Nitrogen, weight % | 0.18 |
| Sulfur, weight % | 1.20 |
| Carbon, weight % | 86.59 |
| Hydrogen, weight % | 12.58 |
| Tenor, ppm | |
| Nickel | 4.7 |
| Vanadium | 5.0 |
| Ferrum | 25.3 |
| Copper | ＜ 0.1 |
| Sodium | 1.8 |
| Boiling range, DEG C | |
| Initial boiling point | 285 |
| 10% | 393 |
| 30% | 470 |
| 50% | 516 |
| 70% | 548 |
| 90% | 581 |
| The end point of distillation | / |
Table 2
| Catalyst is numbered | A |
| Bulk density, kg/m3 | 0.77 |
| Pore volume, ml/g | 0.2 |
| Specific surface area, rice2/ gram | 110 |
| Abrasion index, during weight %-1 | 1.1 |
| Screening composition, weight % | 6 --> |
| 0-40 micron | 15 |
| 40-80 micron | 59 |
| ＞ 80 microns | 26 |
| Fresh catalyst activity | 89 |
| Self regulation time, hour | 40 |
| Equilibrium activity | 58 |
Table 3
It would be recognized that the certain aspects of the invention being for clarity sake described in separate embodiment and feature can also combine offer in single embodiment.On the contrary, for the sake of brevity, the present invention described in the single embodiment various aspects and feature can also be provided separately or provides with any suitable sub combination.
The all publications, patents and patent applications mentioned in this specification is incorporated by this specification through this all in full, is noted specially and one by one just as each publication, patent or patent application and is incorporated herein by this reference.
Although having contacted specific embodiments and embodiment having described the present invention, it will be obvious that those skilled in the art are it can be seen that many replacement schemes, revise and change.Correspondingly, it is intended to contain to fall all such replacement scheme in the spirit and broad scope of claims, revise and change.
Claims (11)
1. one kind is improved the selective processing method of catalytic cracking catalyst, it is characterised in that the method comprises the following steps:
(1), fresh catalyst is loaded fluid bed；
(2), fuel and oxygenous gas are introduced fluid bed, and make fuel generation combustion heat release amount；
(3), it is passed through water vapour and contacts with catalyst, under certain thermal and hydric environment, carrying out aging 1 hour～720 hours；
(4), selective catalyst high after process is joined in industrial catalyticing cracking device.
2. according to the method for claim 1, it is characterized in that described fresh catalyst includes zeolite, inorganic oxide and optional clay, each component accounts for total catalyst weight respectively: zeolite 1 weight %～50 weight %, inorganic oxide 5 weight %～99 weight %, clay 0 weight %～70 weight %, wherein zeolite is selected from mesopore zeolite and/or large pore zeolite.
3., according to the method for claim 1, it is characterised in that aging temperature is 500 DEG C～850 DEG C, the apparent linear velocity of dense-phase fluidized bed is 0.1 meter per second～0.6 meter per second.
4. according to the method for claim 3, it is characterised in that aging temperature is 650 DEG C～790 DEG C, the apparent linear velocity of dense-phase fluidized bed is 0.15 second～0.5 meter per second, and ageing time is 5 hours～360 hours.
5. according to the method for claim 1, it is characterised in that described fuel refers to the material containing C element and/or H element, selected from fuel gas or/and fuel oil.
6. according to the method for claim 5, it is characterised in that described fuel gas includes or is selected from one or more in carbon monoxide, hydrogen, dry gas, liquefied gas, synthesis gas, natural gas, biogas, methane, ethane.
7. according to the method for claim 5, it is characterised in that one or more in gasoline, Petroleum, diesel oil, heavy oil, crude oil, artificial oil of described fuel oil.
8. according to the method for claim 1, it is characterized in that described fluid bed aging temperature control method is as follows: directly light fuel gas combustion system, or spray fuel oil combustion mode, or first make fluidized-bed temperature exceed fuel gas by other heat exchange means or/and ignition temperature, then introduce fuel gas or/and fuel oil.
9. according to the method for claim 1, it is characterised in that it is 0.01%～99.9% that described water vapour accounts for fluid bed gaseous phase volume mark.
10. according to the method for claim 9, it is characterised in that it is 15%～60% that described water vapour accounts for fluid bed gaseous phase volume mark.
11. according to the method for claim 1, it is characterised in that described fluid bed is dense-phase fluidized bed.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
|---|---|---|---|---|
| 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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