CN103725311A - Catalyst regeneration method used for reducing carbon dioxide release and improving selectivity - Google Patents
Catalyst regeneration method used for reducing carbon dioxide release and improving selectivity Download PDFInfo
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Abstract
The invention discloses a catalyst regeneration method used for reducing carbon dioxide release and improving selectivity. The catalyst regeneration method comprises following steps: a carbon-containing catalyst is subjected to partial regeneration in a first regenerator using pure oxygen, and then is delivered into a second regenerator via a U-shaped delivery pipe so as to remove residual coke via combustion using pure oxygen, and smoke obtained from the first regenerator is divided into three parts, wherein a first part of the smoke is cycled into the bottom of the second regenerator, a second part is used for delivering the partially regenerated catalyst from the first regenerator into the second regenerator, and the third part is delivered into a smoke energy recovery system; smoke obtained from the second regenerator and the smoke which is obtained from the first regenerator and is processed via the smoke energy recovery system are combined, are delivered into a carbon dioxide separating system for carbon dioxide separation, and then are collected, and an obtained regenerated catalyst is cooled and activated using a catalyst, and is delivered into a reactor for recycling. The catalyst regeneration method is capable of realizing complete regeneration of the catalyst, reducing carbon release greatly, and even realizing zero carbon release. Catalyst activity distribution is more uniform, so that catalytic cracking product coke yield and dry gas yield are reduced.
Description
Technical field
The present invention relates to the renovation process containing Pd/carbon catalyst in a kind of hydrocarbon processing process.More particularly, the present invention relates to the catalyst regeneration process realizing carbon dioxide discharge-reduction in mink cell focus catalytic cracking process and improve catalyst selectivity.
Background technology
Now, whole world petroleum refining industry development faces the lot of challenges such as oil price fluctuation, the aggravation of crude oil in poor quality trend, oil quality specification improve, energy-saving and emission-reduction requirement becomes sternly, biofuel develops rapidly, and minimizing Carbon emission, mitigation of climate change have become petroleum refining industry transforms mode of economic growth, keeps the only way of Sustainable development.In October, 2009, country has announced the action target of controlling greenhouse gas emission, arrives the year two thousand twenty nationwide units gross domestic product CO
2discharge declined 40% to 45% than 2005, and clearly proposed per GDP carbon dioxide emission reduction 17% during " 12 ", and country likely imposes " carbon tax " during " 12 " in good time simultaneously.Therefore in refining of petroleum and chemical process, effectively reduce carbon emission and seem and be even more important, trap, seal up for safekeeping and manage CO
2refinery's vital task in future will be become.Carbon emission in heavy oil upgrading process is mainly the carbon emission of catalytic cracking burning, hydrogen production process and the energy consumption of technological process.Catalytic cracking unit is the core production equipment of refinery, because catalyzer burns, becomes CO
2one of main source of discharge.
US2011/0155642A1 discloses a kind of catalytic cracking process process that reduces Carbon emission, adopt coke-burning riser series connection dense bed regenerating unit, pure oxygen and the regeneration techniques in coke-burning riser multiple spot delivery of supplemental oxygen, this technology Special attention will be given to has increased a tank in regeneration and circuit to be generated respectively, it is degassed that the tank of circuit of wherein regenerating adopts nitrogen to carry out regenerated catalyst, and the tank of circuit to be generated burns efficiency by temperature before introducing reclaimable catalyst and regenerated catalyst and mixing to improve reclaimable catalyst regeneration to improve.But the introducing of regeneration circuit nitrogen finally inevitably can make nitrogen play a reversed role in flue gas by revivifier, obviously lost the advantage of pure oxygen regeneration, only burn efficiency and increase, but the recovery of carbonic acid gas has increased difficulty.
US4542114 discloses a kind of integral process process that reclaims the flue gas compositions such as carbonic acid gas, can realize and in burning process, go back hydrogen manufacturing and carbon dioxide product, eliminate sulphur, the aerial discharge of oxynitride completely, its pure oxygen mixed gas that adopts carbonic acid gas to dilute carries out catalyzer and burns to produce rich carbonated flue gas simultaneously.But this technique does not increase interior heat collecting device for realizing in revivifier, emphasize wherein the preferred 30-24% of oxygen concentration 60-21% in mixed gas, thereby part has lost the advantage that adopts purity oxygen regeneration, burns efficiency as increased substantially, and reduces revivifier size etc.
US5565089 discloses a kind of catalytic cracking catalyst process of regenerating, first with air, to enter revivifier to carry out catalyzer and burn, then the carbonic acid gas in reclaiming flue gas, recycled carbon dioxide and be incorporated to gradually oxygen-containing gas stream until in revivifier temperature normal, last direct oxygen injection and carbonic acid gas carry out burning of catalyzer.This process of regenerating is only paid close attention to the improvement of regenerative process inlet system aspect and the processing of flue gas, does not consider the problem of the aspects such as revivifier structure or concrete reclaiming process process and catalytic cracking catalyst circulation.
CN1600431A discloses a kind of incomplete regen-eration smoke combustion technology, employing supplements the way of air in the incomplete regen-eration stack gas between catalyst regenerator and flue gas turbine inlet, CO in incomplete regen-eration flue gas is burnt away, thereby make flue-gas temperature be increased to 660-760 ℃, finally make flue gas turbine inlet temperature reach 640-700 ℃, improve cigarette machine organic efficiency, thereby reduce plant energy consumption with recovered flue gas pressure energy to greatest extent.Adopt the present invention, according to the concentration of unit scale and CO and/or entraining hydrocarbon, supplement air capacity 20-300Nm
3/ min, can effectively improve flue-gas temperature 20-80 ℃, improves cigarette engine efficiency.For single hop incomplete regen-eration, in flue, supplement air and also can make flue gas carry hydro carbons secretly fully to burn, eliminate its impact on cigarette machine, but can not effectively reduce CO2 emissions.
Because conventional catalyzer coke burning regeneration method is to pass into air or oxygen-containing gas is regenerated in fluidized-bed, and air is mainly by O
2and N
2composition, contains a large amount of N in the regenerated flue gas therefore producing after catalyzer coke burning regeneration
2, CO
2with a small amount of O
2and CO.And the flue gas of this composition is due to CO
2concentration is low, therefore CO
2separating difficulty is large, cost is high, cannot be isolated collection, can only enter directly discharge after energy-recuperation system, thereby cause Greenhouse effect.
In addition,, from the development of regenerator, pursue the at utmost recovery that realizes regenerated catalyst activity, to realize the maximum conversion ability of hydro carbons always.But the activity of catalyzer is the concept represent of a macroscopical transformation efficiency, does not embody the pursuit of object product selectivity.While for example regenerating, can realize regenerated catalyst activation recovering the highest, but this regenerated catalyst may be because its high reactivity causes high coke and dry gas yied when participating in reaction, this does not wish to see.While therefore regenerating, need to pursue a kind of homogeneity that catalyst activity recovers, realize in other words on regenerated catalyst acid one and be uniformly distributed, thereby realize low coke and dry gas yied, high object product selectivity.Therefore, be necessary to develop a kind of reduction Carbon emission and improve optionally catalyst regeneration process.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of reduces Carbon emission and improves optionally catalyst regeneration process.
Reduction Carbon emission provided by the invention also improves optionally catalyst regeneration process (1) employing block form two device regenerating unit patterns, the first revivifier, Second reactivator are arranged in juxtaposition, between the first revivifier, Second reactivator, by U-shaped catalyst transport, connect, the first revivifier is turbulent bed operation, Second reactivator is bubbling bed operation, and the method comprises:
(1) from the band Pd/carbon catalyst of catalytic cracking unit stripping stage, first in the first revivifier, adopt pure oxygen gas regeneration, coke combustion reactions occurs, the ratio of burning of the first revivifier is 55-65%;
(2) from the first revivifier bottom half regenerated catalyst out, through U-shaped catalyst transport, enter Second reactivator, in Second reactivator bottom, further supplement pure oxygen gas, the catalyzer of incomplete regen-eration is further burnt in dense-phase bed, holomorphosis, the ratio of burning of Second reactivator is 35-45%;
(3) from the first revivifier flue gas out, be divided into three parts, wherein first part's flue gas recirculation is supplemented to Second reactivator bottom; Second section is delivered to Second reactivator by half regenerated catalyst from the first revivifier as delivery medium; Part III enters smoke energy recovering system, and flue gas recirculation need to keep the oxygen concentration in Second reactivator to be not less than 30% being preferably not less than 40%;
(4), from flue gas out of Second reactivator with enter in the lump carbon dioxide separating system from the flue gas of smoke energy recovering system the first revivifier out converges, after separating carbon dioxide, trap;
(5) regenerator sloped tube arranges catalyst activation system, and this system comprises catalyst cooler and activator, enters reactor cycles again use from revivifier regenerated catalyst out after catalyst activation system.
The operational condition of described the first revivifier is: temperature 550-700 ℃, and catalyzer mean residence time is 1.0-4.0 minute preferred 1.0-3.0 minute, the gas superficial linear velocity of the first revivifier is that 0.6-1.0m/s is preferably 0.7-0.9m/s.In the first revivifier, interior heat collector can be set, also can not arrange, depend on whether the temperature of burning tank exceedes 750 ℃.
The operational condition of described Second reactivator is: temperature 580-700 ℃, and catalyzer mean residence time is 1.0-5.0 minute preferred 1.0-4.0 minute, gas superficial linear velocity is that 0.4-0.8m/s is preferably 0.4-0.6m/s.Second reactivator arranges heat collector, to control the temperature of Second reactivator dense-phase bed, is no more than 750 ℃ and is preferably no more than 720 ℃.The heat collector of Second reactivator setting is interior heat collector or/and external warmer, and heat collector is one or more.
The operational condition of described catalyst activation system is: the catalyst cooler similar in activation system is in external warmer, and wherein catalyzer is close operates mutually, and density is 300-700kg/m
3, heat-eliminating medium can be water or other medium.Water cooler need to guarantee that regenerated catalyst temperature after cooling is 550-640 ℃, and optimum is 560-630 ℃.Activator is a fluidizer, and fluidizing medium is middle pressure superheated vapour, and its pressure is 3.0-3.5MPa, and temperature is 400-450 ℃.Catalyzer is close operation mutually in activator, and density is 300-500kg/m
3, the catalyzer residence time is therein 2-8 minute, preferably 3-6 minute.
Described catalyzer comprises zeolite, inorganic oxide and optional clay, and each component accounts for respectively total catalyst weight and is: the heavy % of the heavy %-50 of zeolite 1, the heavy % of the heavy %-99 of inorganic oxide 5, the heavy % of the heavy %-70 of clay 0.Its mesolite is active ingredient, be selected from mesopore zeolite and/or optional large pore zeolite, mesopore zeolite accounts for the heavy % of 10 heavy %-100 of zeolite gross weight, the preferably heavy % of 20 heavy %-80, large pore zeolite accounts for the heavy % of 0 heavy %-90 of zeolite gross weight, the preferably heavy % of 20 heavy %-80.Mesopore zeolite is selected from one or more mixtures and/or the ZRP zeolite in ZSM series zeolite, also can carry out modification to the transition metal such as the non-metallic elements such as phosphorus and/or iron, cobalt, nickel for above-mentioned mesopore zeolite.Large pore zeolite selects one or more the mixture in this group zeolite that super steady Y, high silicon Y that free Rare Earth Y (REY), rare earth hydrogen Y (REHY), different methods obtain form.
Inorganic oxide, as support of the catalyst, is selected from silicon-dioxide and/or aluminium sesquioxide or both mixtures.
Clay, as caking agent, is selected from one or more in kaolin, polynite, diatomite, saponite, rectorite leng, sepiolite, hydrotalcite and wilkinite.
Compared with existing renovation process, major advantage of the present invention is following two aspects:
1, the method not only can make catalyzer holomorphosis, can significantly reduce carbon emission simultaneously, and even zero carbon emission reduces Greenhouse effect.
2, the method can significantly reduce especially revivifier reserve of device catalyst inventory, greatly reduces the size of static equipment and moving equipment, reduces investment, reduces floor space.
3, because purity oxygen concentration in regeneration system rapidly is high, thereby make to burn efficiency, increase substantially, the recovery time shortens, and reduces fragmentation, the wearing and tearing of catalyzer, has improved the service efficiency of catalyzer.
4, the activity that the method can realize regenerated catalyst is uniformly distributed, thereby coke and dry gas yied in the product of catalytic cracking are reduced.
Accompanying drawing explanation
Accompanying drawing is reduction Carbon emission provided by the invention and improves optionally catalyst regeneration process schematic flow sheet.
Embodiment
Below in conjunction with accompanying drawing, further illustrate method provided by the present invention, but the present invention is not therefore subject to any restriction.
Accompanying drawing is reduction Carbon emission provided by the invention and improves optionally catalyst regeneration process schematic flow sheet.
In accompanying drawing, each numbering is described as follows:
1,3,4,7,8,9,10,11,12,17,18,23,27,28,29 all represent pipeline; 2 is the first revivifier; 16 is Second reactivator; 6 is U-shaped catalyst transport; 13,14 and 22 be cyclone separation system; 15 is smoke energy recovering system; 26 is carbon dioxide separating system; 19 is riser reactor; 20 is stripping stage; 21 is settling vessel; 24 is oil and gas separating system; 25 is external warmer; 30 is catalyst cooler; 31 is activator.
As shown in drawings, reclaimable catalyst enters the first revivifier 2 through inclined tube 1 to be generated, and pure oxygen gas also enters the first revivifier 2 through pipeline 3, contacts the combustion reactions of concurrent green coke charcoal with reclaimable catalyst.Incomplete regen-eration catalyzer is from the bottom of the first revivifier 2 through U-shaped catalyst transport 6, by being promoted to Second reactivator 16 through pipeline 12 from the circulating flue gas of the first revivifier.The flue gas of the first revivifier through cyclone separation system 13, pipeline 7 out after, at least a portion enters smoke energy recovering system 15 recovered energies through pipeline 9, another part is divided into two-way, one tunnel goes pipeline 12 as promoting medium, another road enters through pipeline 4 that Second reactivator 16 is auxiliary to be burnt, and can realize the lifting of the carbon dioxide in flue gas concentration that enters carbon dioxide separating system 26 simultaneously.Pure oxygen gas also enters Second reactivator 16 bottoms through pipeline 8 and further burns.Second reactivator arranges external warmer 25 to control Second reactivator temperature.The flue gas of Second reactivator 16 leaves Second reactivator through cyclone separation system 14 and enters carbon dioxide separating system 26 through pipeline 10 with from smoke energy recovering system 15 the first revivifier out flue gas out converges, and realizes the separation and collection of carbonic acid gas.From Second reactivator 16 regenerated catalyst out, through regenerator sloped tube 11, enter catalyst cooler 30, after catalyzer is cooling, by inclined tube 27, enter activator 31, overheated steam also enters activator 31 through pipeline 29, regenerated catalyst after activation enters riser reactor 19 bottoms through inclined tube 28, it is up that pre-lift medium enters riser reactor bottom lifting regenerated catalyst through pipeline 17, stock oil enters riser reactor through pipeline 18 and contacts with regenerated catalyst and carry out catalytic cracking reaction, reaction oil gas is successively through settling vessel 21, cyclone separation system 22 and gas pipeline 23 enter oil and gas separating system 24 and obtain various products.Reclaimable catalyst enters inclined tube 1 to be generated and turns back to the first revivifier 2 and regenerate after stripping stage 20 strippings, thereby realize, recycles.
The following examples will be further described the present invention, but not thereby limiting the invention.The stock oil using in embodiment and comparative example is vacuum residuum, and its character is listed in table 1.Catalyzer is produced by catalyzer branch office of Sinopec Group Shandong catalyst plant, and goods number is MLC-500, and its character is listed in table 2.
Embodiment
Embodiment carries out on catalytic cracking demonstration unit, as shown in drawings.Demonstration unit does not have smoke energy recovering system and carbon dioxide separating system.Wherein 50 centimetres of the internal diameters of the first revivifier dense-phase bed, the internal diameter of Second reactivator dense-phase bed is 40 centimetres.According to renovation process proposed by the invention, catalyzer is regenerated, at the first revivifier and Second reactivator dense-phase bed, pass into respectively pure oxygen gas, from the first revivifier cyclone separation system flue gas part out, return to Second reactivator dense-phase bed bottom simultaneously, another part is as promoting medium transport incomplete regen-eration catalyzer to Second reactivator, last part and go out demonstration unit from Second reactivator flue gas out converges.The bed temperature of the first revivifier is 660 ℃, and Second reactivator dense-phase bed temperature is 670 ℃.Catalyzer is 2 minutes in the residence time of the first revivifier dense-phase bed, at the mean residence time of Second reactivator dense-phase bed, is 3 minutes.The gas superficial linear velocity of the first revivifier is 0.82m/s, and Second reactivator gas superficial linear velocity is 0.54m/s.The density of catalyst of the catalyst cooler in activation system is 550kg/m
3, catalyzer temperature after cooling is 620 ℃.Middle pressure superheated water steaming device pressure 3.4MPa in activation system, 425 ℃ of temperature, density of catalyst 350kg/m in activator
3, the residence time of catalyzer in activator is 3 minutes.Catalyzer from activation system out enters reactor, and the stock oil listed with table 1 contacts, and carries out catalytic cracking reaction, and regeneration condition, reaction conditions, regenerated catalyst carbon content and flue gas composition, products distribution are all listed in table 3.In table 3, flue gas composition is the composition after the first revivifier and Second reactivator flue gas converge.
Comparative example
Comparative example is also to carry out on the catalytic cracking demonstration unit of same structure, there is no smoke energy recovering system and carbon dioxide separating system and catalyst activation system.But the internal diameter of the first revivifier and Second reactivator dense-phase bed is different with embodiment, 200 centimetres of the internal diameters of the first revivifier dense-phase bed, the internal diameter of Second reactivator dense-phase bed is 160 centimetres, other scantlings of the structure is identical with embodiment.Pair reclaimable catalyst identical with embodiment of renovation process routinely regenerated, and the first revivifier and Second reactivator dense-phase bed pass into respectively air, and the bed temperature of the first revivifier is 670 ℃, and Second reactivator dense-phase bed temperature is 710 ℃.Catalyzer is 9 minutes in the residence time of the first revivifier dense-phase bed, at the mean residence time of Second reactivator dense-phase bed, is 12 minutes.The gas superficial linear velocity of the first revivifier is 0.8m/s, and Second reactivator gas superficial linear velocity is 0.5m/s.Catalyzer after regeneration enters reactor, and the stock oil listed with table 1 contacts, and carries out catalytic cracking reaction, and regeneration condition, reaction conditions, regenerated catalyst carbon content and flue gas composition, products distribution are all listed in table 3.In table 3, flue gas composition is the composition after the first revivifier and Second reactivator flue gas converge.
From the result contrast of operational condition and table 3, can find out, compared with comparative example, the present invention significantly reduces, installs general reserve in burning tank size and regeneration dense bed size and significantly reduces, consumes under the obvious prerequisite reducing of wind index, adopt renovation process proposed by the invention, on regenerated catalyst, carbon content reduces more, in addition in the flue gas that, this catalyst regeneration process produces, do not contain CO and N
2, gas concentration lwevel, up to 56.2%, is conducive to separation and the trapping of carbonic acid gas.In addition, embodiment, owing to adopting catalyst activation system, compares ratio dry gas yied and reduces by 0.7 percentage point, and coke yield reduces by 0.9 percentage point, gasoline and diesel yield increase, and total liquid is received (liquefied gas, gasoline, diesel yield sum) increases by 1.5 percentage points.
Table 1
Stock oil title | Vacuum residuum |
Density (20 ℃), kg/m 3 | 920.9 |
Kinematic viscosity, millimeter 2/ second | |
100℃ | 114.4 |
Carbon residue, heavy % | 8.2 |
Condensation point, |
25 |
Total nitrogen, heavy % | 0.33 |
Sulphur, heavy % | 0.21 |
Carbon, heavy % | 86.91 |
Hydrogen, heavy % | 12.55 |
Metal content, ppm | |
Nickel | 8.8 |
Vanadium | 0.1 |
Iron | 1.8 |
Copper | <0.1 |
Sodium | 3.0 |
Boiling range, ℃ | |
HK (initial boiling point) | 415 |
10% | 545 |
30% | / |
50% | / |
70% | / |
KK (final boiling point) | / |
Table 2
Catalyzer goods number | MLC-500 |
Chemical constitution, heavy % | |
Aluminum oxide | 50.2 |
Sodium oxide | 0.321 |
Apparent density, kg/m 3 | 700 |
Pore volume, mL/g | 0.38 |
Specific surface area, m 2/g | 229 |
Abrasion index, during heavy % -1 | 1.9 |
Size composition, heavy % | |
0~40 micron | 17.3 |
40~80 microns | 49.3 |
80 microns of > | 33.4 |
Table 3
Embodiment | Comparative example | |
Device catalyzer general reserve, ton | 1.2 | 6 |
Cracking hydrocarbon reaction member | ||
Outlet temperature of riser, ℃ | 500 | 500 |
Catalyst/feed weight ratio | 6 | 6 |
Reaction times, second | 3 | 3 |
Water vapor/raw material weight ratio | 0.05 | 0.05 |
Products distribution, heavy % | ||
Dry gas | 2.9 | 3.6 |
Liquefied gas | 14.2 | 14.8 |
Gasoline | 39.7 | 38.4 |
Diesel oil | 28.0 | 27.2 |
Heavy oil | 6.7 | 6.6 |
Coke | 8.5 | 9.4 |
Regeneration unit | ||
The first revivifier dense bed internal diameter, cm | 50 | 200 |
Second reactivator dense bed internal diameter, cm | 40 | 160 |
Consumption wind index, Nm 3/kg | 3.7 | 16.8 |
Carbon content on regenerated catalyst, heavy % | 0.01 | 0.06 |
Regenerated flue gas composition, % | ||
N 2 | 0 | 78.62 |
CO 2 | 57.58 | 13.76 |
CO | 0 | 5.73 |
O 2 | 42.42 | 1.89 |
Claims (12)
1. one kind is reduced Carbon emission and improves optionally catalyst regeneration process, it is characterized in that the method adopts block form two device regenerating unit patterns, the first revivifier, Second reactivator are arranged in juxtaposition, between the first revivifier, Second reactivator, by U-shaped catalyst transport, connect, the first revivifier is turbulent bed operation, Second reactivator is bubbling bed operation, and the method comprises:
(1) from the band Pd/carbon catalyst of catalytic cracking unit stripping stage, first in the first revivifier, adopt pure oxygen gas regeneration, coke combustion reactions occurs, the ratio of burning of the first revivifier is 55-65%;
(2) from the first revivifier bottom half regenerated catalyst out, through U-shaped catalyst transport, enter Second reactivator, in Second reactivator bottom, further supplement pure oxygen gas, the catalyzer of incomplete regen-eration is further burnt in dense-phase bed, holomorphosis, the ratio of burning of Second reactivator is 35-45%;
(3) from the first revivifier flue gas out, be divided into three parts, wherein first part's flue gas recirculation is supplemented to Second reactivator bottom; Second section is delivered to Second reactivator by half regenerated catalyst from the first revivifier as delivery medium; Part III enters smoke energy recovering system, and flue gas recirculation need to keep the oxygen concentration in Second reactivator to be not less than 30% being preferably not less than 40%;
(4), from flue gas out of Second reactivator with enter in the lump carbon dioxide separating system from the flue gas of smoke energy recovering system the first revivifier out converges, after separating carbon dioxide, trap;
(5) regenerator sloped tube arranges catalyst activation system, and this system comprises catalyst cooler and activator, enters reactor cycles again use from revivifier regenerated catalyst out after catalyst activation system.
2. according to the method for claim 1, it is characterized in that the operational condition of described the first revivifier is: temperature 550-700 ℃, catalyzer mean residence time is 1.0-4.0 minute, gas superficial linear velocity is 0.4-0.8m/s.
3. according to the method for claim 2, it is characterized in that the operational condition of described the first revivifier is: catalyzer mean residence time is 1.0-3.0 minute, gas superficial linear velocity is 0.7-0.9m/s.
4. according to the method for claim 1, it is characterized in that the operational condition of described Second reactivator is: temperature 580-700 ℃, catalyzer mean residence time is 1.0-5.0 minute, gas superficial linear velocity is 0.4-0.8m/s.
5. according to the method for claim 4, it is characterized in that the operational condition of described Second reactivator is: catalyzer mean residence time is 1.0-4.0 minute, gas superficial linear velocity is 0.4-0.6m/s.
6. according to the method for claim 1, it is characterized in that Second reactivator arranges heat collector, to control the temperature of Second reactivator dense-phase bed, be no more than 750 ℃, described heat collector is interior heat collector or/and external warmer, and heat collector is one or more.
7. according to the method for claim 6, it is characterized in that the temperature of controlling Second reactivator dense-phase bed is no more than 720 ℃.
8. according to the method for claim 1, it is characterized in that the oxygen concentration in the described flue gas of step (3) is not less than 40%.
9. according to the method for claim 1, it is characterized in that catalyzer close operation mutually in described catalyst cooler, density is 300-700kg/m
3.
10. according to the method for claim 1, it is characterized in that catalyzer close operation mutually in described activator, density is 300-500kg/m
3, the catalyzer residence time is therein 2-8 minute; Fluidizing medium is middle pressure superheated vapour, and its pressure is 3.0-3.5MPa, and temperature is 400-450 ℃.
11. according to the method for claim 10, it is characterized in that the residence time of catalyzer in described activator is 3-6 minute.
12. according to the method for claim 1, it is characterized in that described catalyzer comprises zeolite, inorganic oxide and optional clay, each component accounts for respectively total catalyst weight and is: the heavy % of the heavy %-50 of zeolite 1, the heavy % of the heavy %-99 of inorganic oxide 5, the heavy % of the heavy %-70 of clay 0.
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CN108698040A (en) * | 2016-03-31 | 2018-10-23 | 环球油品公司 | FCC counter-current regeneration devices |
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CN108698040A (en) * | 2016-03-31 | 2018-10-23 | 环球油品公司 | FCC counter-current regeneration devices |
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