CN103028449A - Catalytic conversion catalyst regenerator - Google Patents
Catalytic conversion catalyst regenerator Download PDFInfo
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- CN103028449A CN103028449A CN2011102910296A CN201110291029A CN103028449A CN 103028449 A CN103028449 A CN 103028449A CN 2011102910296 A CN2011102910296 A CN 2011102910296A CN 201110291029 A CN201110291029 A CN 201110291029A CN 103028449 A CN103028449 A CN 103028449A
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Abstract
A catalytic conversion catalyst regenerator comprises a regeneration zone, a settling zone, a buffer zone and an optional cooling zone, wherein the buffer zone is adjacent to the regeneration zone, the buffer zone is provided with a catalyst inlet and a catalyst outlet, and the catalyst inlet is connected with the cooling zone or/and an inclined tube to be regenerated, and is preferably connected with the cooling zone; and the catalyst outlet is connected with a regeneration inclined tube. A catalytic conversion catalyst regeneration method comprises the following steps: a catalyst to be regenerated enters the regeneration zone of the regenerator, contacts with an oxygen-containing gas, and undergoes a combustion reaction, the obtained regenerated catalyst enters the buffer zone, is cooled, and is returned to a reactor, and a flue gas is discharged from the top of the settling zone. The buffer zone adopted in the invention enables the catalyst temperature distribution to be uniform, has a cooling effect on the dilute phase of the regenerator, and allows the overheat phenomenon of the dilute phase to difficultly appear.
Description
Technical field
The present invention relates to contain in the catalytic cracking process regenerator that Pd/carbon catalyst burns.
Background technology
Feedstock oil owing to there being condensation reaction, except generating light hydrocarbons, also generates a part of coke when carrying out catalytic cracking reaction, reduce thereby be deposited on the activity and selectivity that makes catalyst on the catalyst.Therefore, adopt the high-temperature oxydation renovation process, the burning of the coke on the catalyst is removed to recover the serviceability of catalyst, this process is called the regeneration of catalyst, usually the catalyst with deposit coke is called reclaimable catalyst, and the catalyst behind the oxidation regeneration is called regenerated catalyst.Burning process is finished in regenerator, can be divided into turbulent bed, fast bed and conveying bed etc. according to regenerator fluid bed type difference; Can be divided into completing combustion and partial combustion according to the CO burning degree; Can be divided into and stream, cross-flow and adverse current are burnt according to catalyst is different with the Air for burning coke flow process; Can be divided into single hop and two-stage regeneration according to burning the fluidized bed region difference; Can be divided into single device, two devices and many devices according to the difference of burning regional container burns.Catalytic cracking regenerator generally comprises the regeneration function district of regenerating for reclaimable catalyst, the sedimentation function district that is used for the sedimentation catalyst and places gas-solid separator, along with the propelling of RFCC, regenerator has increased the cooling function district with catalyst heat-obtaining function.
Early stage catalyst recovery process is to pass into oxygen-containing gas in low speed circulating fluidized bed, and employing single hop regeneration, in the fluid bed of this low linear speed, the full back-mixing of gas-solid, gas and solid contacting efficiency are low, and catalyst regeneration speed is slow, have caused the regenerator catalyst inventory excessive, the regeneration effect of catalyst is poor, the regenerated catalyst carbon content is approximately 0.2 to weigh %, and coke burning degree is low, is about 100kg (amount of coke)/[h (unit interval) T (catalyst inventory)].Along with molecular sieve catalyst uses on catalytic cracking unit widely, the especially use of the molecular sieve catalyst of USY type, carbon content and regeneration remaining on the regenerated catalyst are very large on activity and the selective impact that recovers catalyst.Therefore, effectively reduce catalyst inventory in the regenerative process and improve the direction that the catalyst regeneration effect becomes the regeneration techniques exploitation.This is because in service at catalytic cracking unit, catalyst constantly is subject to the effect of high temperature and water vapour, the heavy metal deposition that carries in the feedstock oil is on catalyst surface, the active of catalyst constantly reduces, need fresh makeup catalyst to keep the equilibrium activity of catalyst in reaction-regeneration system, when one timing of fresh catalyst magnitude of recruitment, the catalyst general reserve is lower in the reaction-regeneration system, the catalyst replacement rate is just higher, and the equilibrium activity of reaction-regeneration system catalyst is also just higher so.
USP3563911 discloses a kind of two-stage regeneration, reclaimable catalyst is sequentially by the first dense-phase fluidized bed and the second dense-phase fluidized bed, contact with oxygen containing gas and to make coke generation combustion reaction on the catalyst surface, the flue gas that produces mixes and entrained catalyst enters the dilute phase settling section.The first dense-phase fluidized bed regeneration temperature is greater than 1050 °F (namely 565.5 ℃); The gas superficial linear velocity of the second dense-phase fluidized bed is 1.25 feet per seconds～6 feet per seconds (i.e. 0.381 meter per second～1.83 meter per seconds), and regeneration temperature is 1125～1350 °F (namely 607.2～732.2 ℃).The method is compared with catalyst single hop renovation process, and under the not high condition of regenerative process carbon-burning load, it is nearly 40% that the reserve of regenerator inner catalyst can reduce, and the carbon content of regenerated catalyst can be lower than 0.1 % by weight.
CN1052688A discloses a kind of two-stage oxidizing regenerative method of fluid catalyst, reclaimable catalyst contacts the combustion reaction of concurrent green coke charcoal with oxygen containing gas in the first dense-phase fluidized bed, the gas superficial linear velocity of the first dense-phase fluidized bed is 0.8～2.5 meter per second, the catalyst mean residence time is 0.6～1.0 minute, and regeneration temperature is 650～750 ℃; Catalyst is removed most of coke in the first fluidized bed after, the catalyst of partial regeneration and gas pass distributor together and on flowing to, enter the second fluid bed, contact again the combustion reaction of concurrent green coke charcoal with oxygen containing gas, the gas superficial linear velocity of the second dense-phase fluidized bed is 1.2～3.0 meter per seconds, the catalyst mean residence time is 1.0～2.2 minutes, regeneration temperature is 700～800 ℃, after catalyst is fully regenerated, regenerated catalyst separates with flue gas, part regenerated catalyst enters reactor, and another part regenerated catalyst turns back to the first fluidized bed.
CN1221022A discloses a kind of lapping type two-stage regeneration technology of heavy oil fluidized catalystic cracking, the method comprises two regenerators of arranged superposed, one section regeneration is upper, the temperature of first paragraph is 650～720 ℃, two sections regeneration are lower, the temperature of second segment regenerator is 650～780 ℃, be connected as a single entity with the low pressure drop distribution grid between two regenerators, and two regenerators only need be with a flue and double slide valve or butterfly valve.The regenerative agent phosphorus content is 0.01～0.1% weight.
Develop from regeneration techniques, the development goal of regeneration techniques is under the catalyst deactivation environment and abrasive conditions that relatively relax always, the regenerated catalyst carbon content is controlled at below 0.10 % by weight, be preferably lower than 0.05 % by weight, coke burning degree is brought up to more than the 100kg/ (th), reach the highest with realization regenerated catalyst activation recovering, thereby the conversion capability of realizing hydro carbons is maximum.Therefore, adopt highly active zeolite catalyst after, regenerator superficial gas flow velocity increases to more than 0.6 meter per second, coke burning degree is brought up to more than the 100kg/ (th), the catalyst time of staying is below 4 minutes, and regeneration temperature need to be kept enough height and burn temperature, burns dynamics with improvement.But very important is when regeneration temperature is high, the first Contact Temperature of regenerated catalyst and feedstock oil improves thereupon, the problem that dry gas and coke yield increase easily appears, in addition because regenerated catalyst temperature is higher, the oil ratio of therefore corresponding catalytic cracking unit descends the heavy oil conversion performance variation thereupon.In order to alleviate this contradiction, the cooling catalyst technology is paid close attention to gradually.
US3679576 discloses a kind of fluid catalytic cracking equipment and process, and this technique is mixed the purpose that reaches the reduction catalyst temperature by reclaimable catalyst and regenerated catalyst, thereby reaches the increase conversion ratio, reduces the purpose of dry gas and coke yield.
US5451313 discloses the recirculation reactor that catalytically cracked material contacts with catalyst, this reactor at first allows and mixes in the mixed zone that is positioned at catalytic cracking unit riser bottom from the reclaimable catalyst of reactor stripper with from the regenerated catalyst of regenerator, reach the purpose that reduces catalyst temperature, then the catalyst after the cooling contacts with feedstock oil and carries out catalyzed conversion, thereby reaches the purpose that increases conversion ratio and reduce dry gas and coke.
CN101665713A provides a kind of round-robin method and equipment thereof of cold regenerated catalyst, from the regenerated catalyst of regenerator through catalyst cooler be cooled to 200 ℃～720 ℃ not with or with enter riser reactor after another part mixes without the hot regenerated catalyst of cooling, hydrocarbon raw material increases conversion ratio and the purpose that reduces dry gas and coke in riser reactor and catalyst haptoreaction thereby reach.
CN101191071A and CN101191072A provide the regenerated catalyst thermoregulation equipment of catalytic cracking unit, its main method is that regenerated catalyst is introduced the cooling catalyst district, carry out heat-obtaining at cooling area by heat collector, then the catalyst after the cooling contacts with feedstock oil and carries out catalyzed conversion, thereby reaches the purpose that increases conversion ratio and reduce dry gas and coke.
CN101104816A discloses a kind of regenerated catalyst thermoregulation device for catalytic cracking equipment, the sidewall of regenerator dense bed is provided with catalyst and extracts mouth and hot regenerated catalyst extraction mouth out, the cooling catalyst device is extracted mouth out by catalyst and is connected with the regenerator dense bed, the pre-lift blender that is arranged on riser reactor conversion zone bottom is connected with the cooling catalyst device by cold regenerated catalyst carrier pipe and cold regeneration guiding valve, is connected with the regenerator dense bed by hot regenerated catalyst carrier pipe and heat regeneration guiding valve.The method can make the oil ratio in the catalytic cracking reaction process improve flexibly.
The appearance of Novel cold thermocatalyst hybrid cooling functional areas has realized that to a certain extent catalytic cracking unit improves the purpose that product distributes.But when needs increased substantially the internal circulating load of catalyst, existing catalyst mix falling temperature technique can't stably provide all uniform catalyst of even fluidisation of heat for riser reactor.For the completing combustion mode, when carbon monoxide does not have in mutually completing combustion to rise to the dilute phase burning tail combustion phenomenon can to occur close, the reason that occurs mainly comprises the main air skewness, catalyst fluidization is bad, dense-phase bed is excessively low, fresh catalyst replenish too fast, combustion adjuvant is not enough, the external warmer return catalizer detours etc., the dilute phase temperature often rose rapidly after the tail combustion occured, approach or surpass 800 ℃, thereby make the regenerator overtemperature.The regenerator overtemperature can damage equipment, inner member and lining in the settler, causes pressure oscillation, can affect the device even running if deal with improperly.If adopt platinum based carbon monoxide combustion adjuvant, can be because the catalytic action of platinum causes catalytic cracking unit NOx discharging to increase.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of catalytic converting catalyst regenerator, to prevent the regenerator overtemperature, stably provide lower temperature and the uniform catalyst of heat for riser reactor.
Catalytic converting catalyst regenerator provided by the invention comprises renewing zone, decanting zone, buffering area and optional cooling area, and wherein said buffering area is adjacent with described renewing zone.
Described renewing zone is for reclaimable catalyst activity recovery functional area.The renewing zone can be established one or more.The renewing zone is provided with catalyst inlet and catalyst outlet, and wherein catalyst inlet links to each other with inclined tube to be generated, and catalyst outlet, preferably links to each other with cooling area or/and regenerated catalyst pipe links to each other with cooling area.One or more catalyst dispensers are set in the renewing zone are used for distributing catalyst, one or more main air distributors such as distribution grid or distributor pipe also are set in the renewing zone, be used for distribution oxygen-containing gas (being also referred to as main air).
Described decanting zone is for catalyst sedimentation or/and place the gas-solid separation equipment functional area, and catalyst is the gas phase fluidization state in this district, also claims this district to be dilute-phase zone, and exhanst gas outlet is established at the top, decanting zone.Respectively distinguish when arranged vertically when regenerator, generally the decanting zone is arranged on topmost.
Described buffering area is the interim memory function district for outer defeated catalyst, and buffering area is provided with catalyst inlet and catalyst outlet, and wherein catalyst inlet, preferably links to each other with cooling area or/and inclined tube to be generated links to each other with cooling area; Catalyst outlet links to each other with regenerator sloped tube.
Described buffering area is adjacent with described renewing zone.Respectively distinguish when arranged vertically when regenerator, the position of buffering area can arrange flexibly, both can be below the renewing zone, also can be on the renewing zone, and also can be in the middle of a plurality of renewing zones.One or more catalyst dispensers are set in the buffering area are used for distributing catalyst, one or more fluidizing agent distributors also are set in the buffering area are used for the distribution fluidizing agent.
Described cooling area is to reduce the temperature function district for high temperature catalyst, and regenerator can arrange cooling area, also cooling area can be set, and cooling area preferably is set.Cooling area is located between buffering area and the renewing zone.In cooling area, adopt the mode of heat collector that catalyst is carried out the heat-obtaining cooling.
Renewing zone, decanting zone, buffering area and optional cooling area can arrange a plurality of, for example one or more renewing zones can be set, and also a cooling area or a plurality of cooling areas etc. can be set.Can be connected to each other directly for the identical function district, also can directly not connect.
Renewing zone, decanting zone, buffering area and the connected mode of being connected cooling area wantonly are selected from one or more in connecting of wall connection, tubular type connection, board-like connection, gas-solid separator, wherein tubular type connects one or more that are selected from the connection of dilute phase pipe, distributor pipe connection, carrier pipe connection, the T-shaped pipe, board-like connection preferred distribution plate connects, and gas-solid separator connects preferred cyclone separator or/and thick cyclone separator.
Catalytic converting catalyst renovation process provided by the invention comprises: reclaimable catalyst enters the regenerator renewing zone, contact the generation combustion reaction with oxygen-containing gas, the gained regenerated catalyst enters buffering area, and regenerated catalyst is Returning reactor after cooling, and flue gas is discharged from the top, decanting zone.
In the renewing zone, described catalyst mean residence time is 0.5～30 minute, is preferably 1.5～10 minutes; Described temperature is 600～900 ℃, is preferably 650～750 ℃; Described gas superficial linear velocity is 0.2～5.0 meter per second, is preferably 0.5～3.5 meter per second; The catalyst carbon content is 0.15～0.8 heavy %, is preferably 0.17～0.5 heavy %.
In buffering area, described catalyst mean residence time is 0.5～30 minute, is preferably 1～10 minute; Described temperature is 200～700 ℃, is preferably 500～680 ℃; Described gas superficial linear velocity is 0.1～4.0 meter per second, is preferably 0.2～0.9 meter per second.
The buffering area fluidizing agent is selected from one or more in inert gas, oxidizing gas, the reducibility gas, wherein inert gas is that steam is or/and carbon dioxide containing gas, oxidizing gas is air or/and oxygen-containing gas, and reducibility gas is selected from dry gas, contains CO gas, in the flue gas one or more.
The buffering area catalyst is selected from one or more in cooling area, renewing zone, the stripping rear catalyst.
The employing regeneration is selected from one or more in holomorphosis mode, the incomplete regen-eration mode in the renewing zone.
The invention has the advantages that:
1, the buffering area catalyst temperature is evenly distributed, and the separate sources catalyst mix is even.
2, the heavy metal on the catalyst surface is under low temperature and long-time operation condition, and the part heavy metal is buried by matrix, and remaining part heavy metal is passivated.
3, buffering area has cooling-down effect for the regenerator dilute phase, is not easy to occur the dilute phase overheating problem.
Description of drawings
Fig. 1,2,3,4,5 is to be the basic equipment schematic diagram of five kinds of embodiments provided by the invention.
The specific embodiment
Further specify Apparatus and method for provided by the present invention below in conjunction with accompanying drawing, but the present invention is not therefore subject to any restriction.
Embodiment one:
Fig. 1 is the basic equipment schematic diagram of embodiment one provided by the invention.
As shown in Figure 1, buffering area 1, renewing zone 2 and decanting zone 4 are arranged vertically from bottom to top, and cooling area 5 is listed between renewing zone 2 and the buffering area 1, and renewing zone 3 is the single hop regeneration, and the direct-connected mode of wall is adopted in renewing zone 2 and decanting zone 4.Come the reclaimable catalyst of autoreactor to enter renewing zone 2 through inclined tube 6 to be generated and be uniformly distributed in dense bed top through distributor, 2 bottom enters and upwards flows main air from the renewing zone by main air distributing plate 10 through pipeline 11, with the concurrent green coke charcoal of the reclaimable catalyst counter current contacting combustion reaction that flows downward by gravity, catalyst activity is restored, flue gas is successively through the decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating among the figure), part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collectors, fluidizing agent 13 enters from the bottom of buffering area 1 through fluidizing agent distributor 12 the cooling rear catalyst is carried out fluidisation, fluidizing agent gas in the buffering area 1 enters decanting zone 4 through balance pipe 16, and the regenerated catalyst in the buffering area 1 enters riser reactor through regenerator sloped tube 7 and contacts generation catalytic cracking reaction (indicating among the figure) with feedstock oil.
Embodiment two:
Fig. 2 is the basic equipment schematic diagram of embodiment two provided by the invention.
As shown in Figure 2, buffering area 1, renewing zone 2, renewing zone 3 and decanting zone 4 are arranged vertically from bottom to top, cooling area 5 is listed between renewing zone 2, renewing zone 3 and the buffering area 1, and renewing zone 2 and 3 is band burning tank regeneration, and the direct-connected mode of wall is adopted in renewing zone 3 and decanting zone 4.The reclaimable catalyst that comes autoreactor enters through inclined tube 6 to be generated and burns 2 bottoms, pot type renewing zone and mix with high temperature catalyst that circulation pipe 14 returns and improve catalysis reclaimable catalyst temperature, main air is entered from the bottom of burning pot type renewing zone 2 by main air distributing plate 10 through pipeline 11, mix rear catalyst with oxygen-containing gas with the fast bed form upwards, oxygen-containing gas contacts the combustion reaction of concurrent green coke charcoal with mixed catalyst under higher temperature, be restored near 80% above catalyst activity, half regenerated catalyst and flue gas are successively through the dilute phase pipe, thick cyclone separator separates half regenerated catalyst (not indicating among the figure) with flue gas, catalyst falls into renewing zone 3 dense-phase bed, send into oxygen-containing gas in dense-phase bed, make half regenerated catalyst be in fluidized state and proceed coke burning regeneration, a part of high temperature catalyst returns in 2 burning tanks of renewing zone through circulation pipe 14 heat is provided in 3 dense-phase bed of renewing zone, flue gas is through the decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating among the figure), part regenerated catalyst enters buffering area 1 after cooling area 5 coolings, fluidizing agent 13 makes the cooling catalyst be in fluidized state through the bottom that fluidizing agent distributor 12 enters buffering area 1, fluidizing agent gas enters decanting zone 4 through balance pipe 16 in the buffering area 1, and a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and contacts generation catalytic cracking reaction (indicating among the figure) with feedstock oil in the buffering area 1.
Embodiment three:
Fig. 3 is the basic equipment schematic diagram of embodiment three provided by the invention.
As shown in Figure 3, renewing zone 2, buffering area 1 and decanting zone 4 are arranged vertically from bottom to top, and cooling area 4 is listed between renewing zone 2 and the buffering area 1, and renewing zone 2 is the single hop regeneration, and the direct-connected mode of wall is adopted in buffering area 1 and decanting zone 4.Come the reclaimable catalyst of autoreactor to enter renewing zone 2 through inclined tube 6 to be generated and be uniformly distributed in dense bed top through distributor, 2 bottom enters and upwards flows main air from the renewing zone by main air distributing plate 10 through pipeline 11, with the concurrent green coke charcoal of the reclaimable catalyst counter current contacting combustion reaction that flows downward by gravity, catalyst activity is restored, flue gas enters buffering area 1 so that buffering area cooling catalyst is in fluidized state through macropore distribution grid 11, part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collectors, high-temperature flue gas after the cooling of buffering area 1 cooling catalyst successively through the decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating among the figure), a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and contacts generation catalytic cracking reaction (indicating among the figure) with feedstock oil in the buffering area 1, and another part regenerated catalyst returns renewing zone 2 through regenerated catalyst pipe 14 and is used for the control regeneration temperature.
Embodiment four:
Fig. 4 is the standby schematic diagram of substantially putting of embodiment four provided by the invention.
As shown in Figure 4, renewing zone 3, renewing zone 2, buffering area 1 and decanting zone 4 are arranged vertically from bottom to top, cooling area 5 is listed between renewing zone 3 and the buffering area 1, and renewing zone 2 and renewing zone 3 are the two-stage regeneration mode, and the direct-connected mode of wall is adopted in buffering area 1 and decanting zone 4.The reclaimable catalyst that comes autoreactor enters turbulent bed renewing zone 2 through inclined tube 6 to be generated and is uniformly distributed in the oxygen-containing gas of dense bed top and bottom sending into through distributor and carries out oxygen deprivation regeneration, high-temperature flue gas after the cooling of buffering area 1 cooling catalyst successively through the decanting zone 4, cyclone separator 8, flue gas pipeline 9 enters smoke energy recovering system (not indicating among the figure), half regenerated catalyst is drawn 2 bottoms from the renewing zone, enter turbulent bed renewing zone 3 through half regenerated catalyst pipe 15,3 bottom enters and carries out oxygen enrichment regeneration main air from the renewing zone by main air distributing plate 10 through pipeline 11, the remaining coke of burning-off, catalyst activity is restored, renewing zone 3 flue gases enter renewing zone 2 through top macropore distribution grid (not indicating among the figure), excess oxygen in the flue gas 2 continues to burn utilization in the renewing zone, part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collectors, a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and contacts generation catalytic cracking reaction (indicating among the figure) with feedstock oil in the buffering area 1.
Embodiment five:
Fig. 5 is the basic equipment schematic diagram of embodiment five provided by the invention.
As shown in Figure 5, buffering area 1, renewing zone 2 and decanting zone 4 are arranged vertically from bottom to top, and renewing zone 2 is the single hop regeneration, and the direct-connected mode of wall is adopted in renewing zone 2 and decanting zone 4.Come the reclaimable catalyst of autoreactor to enter renewing zone 2 through inclined tube 6 to be generated and be uniformly distributed in dense bed top through distributor, 2 bottom enters and upwards flows main air from the renewing zone by main air distributing plate 10 through pipeline 11, with the concurrent green coke charcoal of the reclaimable catalyst counter current contacting combustion reaction that flows downward by gravity, catalyst activity is restored, flue gas is successively through the decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating among the figure), part high-temperature regenerated catalyst enters buffering area 1 through regenerated catalyst pipe 14, part reclaimable catalyst enters buffering area 1 through inclined tube 17 to be generated through old catalyst distrbutor, mix with high temperature catalyst, fluidizing agent 13 enters from the bottom of buffering area 1 through fluidizing agent distributor 12 mixed catalyst is carried out fluidisation, fluidizing agent gas enters renewing zone 2 through dilute phase pipe 18 in the buffering area 1, and a part of mixed catalyst enters riser reactor through regenerator sloped tube 7 and contacts generation catalytic cracking reaction (indicating among the figure) with feedstock oil in the buffering area 1.
The following examples will be further described the present invention, but not thereby limiting the invention.Employed feedstock oil is the vacuum gas oil (VGO) (mixing slag gas oil) of mixing decompression residuum in embodiment and the Comparative Examples, and its character is listed in table 1.Catalyst is produced by catalyst branch company of Sinopec Group, and goods number is CGP-1.
The present embodiment carries out at kitty cracker, as shown in Figure 3.Regenerate according to regenerator proposed by the invention, namely the renewing zone is adverse current single hop regeneration, and the heat-obtaining rear catalyst enters buffering area, the main operating condition of regenerator and the results are shown in Table 2.
Comparative Examples 1
Comparative Examples 1 also is to carry out at the kitty cracker identical with embodiment 1, the adverse current single hop renovation process pair reclaimable catalyst identical with embodiment routinely regenerated, when adopting Comparative Examples, tail combustion problem easily appears when regeneration temperature is brought up to 650～680 ℃, be quiet run, can't continue to improve regeneration temperature, the main operating condition of regenerator and the results are shown in Table 2.
As can be seen from Table 2, compare with Comparative Examples 1, because the present invention adopts buffering area, so that regenerator tail combustion phenomenon is resolved, renewing zone of the present invention regeneration temperature obviously improves, reach 700 ℃, catalyst burn efficient be improved significantly, carbon content can reach 0.06 heavy % on the catalyst, be delivered to the reactor catalyst temperature and can be reduced to as required 660 ℃, under the riser reactor raw material preheating temperature condition identical with oil ratio, outlet temperature of riser can be reduced to 505 ℃ from 515 ℃ of Comparative Examples 1.
The present embodiment carries out at kitty cracker, as shown in Figure 3.Regenerate according to regenerator proposed by the invention, namely the renewing zone is adverse current single hop regeneration, and heat-obtaining rear catalyst and part reclaimable catalyst enter buffering area to be mixed, the main operating condition of regenerator and the results are shown in Table 3.
Comparative Examples 2
Comparative Examples 2 also is to carry out at the kitty cracker identical with embodiment 2, the adverse current single hop renovation process pair reclaimable catalyst identical with embodiment routinely regenerated, when adopting Comparative Examples 2, tail combustion problem easily appears when regeneration temperature is brought up to 650～680 ℃, be quiet run, can't continue to improve regeneration temperature, the main operating condition of regenerator and the results are shown in Table 3.
As can be seen from Table 3, compare with Comparative Examples 2, because the present invention adopts buffering area, so that regenerator tail combustion phenomenon is resolved, renewing zone of the present invention regeneration temperature obviously improves, reach 710 ℃, catalyst burn efficient be improved significantly, carbon content can be controlled at 0.18 heavy % as required on the mixed catalyst, be delivered to the reactor catalyst temperature and can be reduced to as required 660 ℃, riser reactor is under the fuel oil preheating temperature condition identical with outlet temperature, and oil ratio can bring up to 8.0 from 6.0 of Comparative Examples 2.
Table 1
| The feedstock oil title | Mix slag gas oil |
| Density (20 ℃), kg/m 3 | 906.0 |
| Kinematic viscosity, millimeter 2/ second | |
| 80℃ | 32.45 |
| 100℃ | 12.35 |
| Carbon residue, heavy % | 3.3 |
| Condensation point, ℃ | 28 |
| Acid number, mgKOH/g | 1.42 |
| Total nitrogen, heavy % | 0.18 |
| Sulphur, heavy % | 0.57 |
| Carbon, heavy % | 87.21 |
| Hydrogen, heavy % | 12.04 |
| Tenor, ppm | |
| Nickel | 24.9 |
| Vanadium | 0.7 |
| Iron | 4.4 |
| Copper | 0.7 |
| Sodium | 1.8 |
| Boiling range, ℃ | |
| HK (initial boiling point) | 316 |
| 10％ | 354 |
| 30％ | 415 |
| 50％ | 450 |
| 70％ | 493 |
| KK (end point of distillation) | 520 |
Table 2
| |
Comparative Examples 1 | |
| Regenerator | ||
| The renewing zone | ||
| Gas superficial velocity, meter per second | 0.9 | 0.9 |
| The catalyst time of staying, minute | 5.9 | 5.9 |
| The regeneration dense phase temperature, ℃ | 700 | 680 |
| Buffering area | ||
| Gas superficial velocity, meter per second | 0.4 | / |
| The catalyst time of staying, minute | 2.0 | / |
| Catalyst temperature, ℃ | 660 | / |
| The decanting zone | ||
| The dilute phase temperature, ℃ | 671 | 720 |
| Cooling area | ||
| Cooling method | The up flow type external warmer | The downflow system external warmer |
| Be delivered to reactor catalyst | ||
| Carbon content on the catalyst, heavy % | 0.06 | 0.20 |
| Catalyst temperature, ℃ | 660 | 680 |
| Reactor | ||
| The fuel oil preheating temperature, ℃ | 330 | 330 |
| Oil ratio, m/m | 4.5 | 4.5 |
| Outlet temperature of riser, ℃ | 505 | 515 |
Table 3
| |
Comparative Examples 2 | |
| Regenerator | ||
| The renewing zone | ||
| Gas superficial velocity, meter per second | 0.9 | 0.9 |
| The catalyst time of staying, minute | 3.0 | 5.9 |
| The regeneration dense phase temperature, ℃ | 710 | 680 |
| Buffering area | ||
| Gas superficial velocity, meter per second | 0.3 | / |
| The catalyst time of staying, minute | 4.0 | / |
| Catalyst temperature, ℃ | 660 | / |
| The decanting zone | ||
| The dilute phase temperature, ℃ | 660 | 720 |
| Cooling area | ||
| Cooling method | The downflow system external warmer | The downflow system external warmer |
| Be delivered to reactor catalyst | ||
| Carbon content on the catalyst, heavy % | 0.18 | 0.20 |
| Catalyst temperature, ℃ | 660 | 680 |
| Reactor | ||
| The fuel oil preheating temperature, ℃ | 200 | 200 |
| Oil ratio, m/m | 8.0 | 6.0 |
| Outlet temperature of riser, ℃ | 505 | 505 |
Claims (9)
1. the catalytic converting catalyst regenerator is characterized in that this regenerator comprises renewing zone, decanting zone and buffering area, and wherein said buffering area is adjacent with described renewing zone.
2. the catalytic converting catalyst regenerator is characterized in that this regenerator comprises renewing zone, decanting zone, buffering area and cooling area, and wherein said buffering area is adjacent with described renewing zone.
3. according to the regenerator of claim 1 or 2, it is characterized in that described buffering area is provided with catalyst inlet and catalyst outlet, wherein catalyst inlet, preferably links to each other with cooling area or/and inclined tube to be generated links to each other with cooling area; Catalyst outlet links to each other with regenerator sloped tube.
4. according to the regenerator of claim 3, the catalyst inlet that it is characterized in that described buffering area with link to each other with cooling area.
5. according to the regenerator of claim 1 or 2, it is characterized in that described buffering area arranges one or more fluidizing agent distributors.
6. according to the regenerator of claim 2, it is characterized in that described cooling area is heat collector, cooling area is located between buffering area and the renewing zone.
7. according to the regenerator of claim 1 or 2, it is characterized in that described renewing zone is provided with catalyst inlet and catalyst outlet, wherein catalyst inlet links to each other with inclined tube to be generated, and catalyst outlet, preferably links to each other with cooling area or/and regenerated catalyst pipe links to each other with cooling area.
8. according to the regenerator of claim 7, the catalyst outlet that it is characterized in that described renewing zone with link to each other with cooling area.
9. according to the regenerator of claim 1 or 2, the connected mode that it is characterized in that described renewing zone, decanting zone, buffering area and be connected cooling area wantonly is selected from one or more in connecting of wall connection, tubular type connection, board-like connection, gas-solid separator, wherein tubular type connects one or more that are selected from the connection of dilute phase pipe, distributor pipe connection, carrier pipe connection, the T-shaped pipe, board-like connection preferred distribution plate connects, and gas-solid separator connects preferred cyclone separator or/and thick cyclone separator.
Priority Applications (1)
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| CN104549566A (en) * | 2013-10-17 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regenerator and regeneration method |
| CN106890681A (en) * | 2017-04-20 | 2017-06-27 | 上海蓝科石化环保科技股份有限公司 | A kind of catalytic cracked regenerated system and method |
| WO2018196361A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Fluidized bed apparatus and method for preparing para-xylene co-produced low-carbon olefin from methanol and/or dimethyl ether and toluene |
| CN113231109A (en) * | 2021-04-25 | 2021-08-10 | 西安航天源动力工程有限公司 | Waste catalyst regeneration reaction furnace |
| US11084765B2 (en) | 2017-04-27 | 2021-08-10 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene |
| US11311852B2 (en) | 2017-04-27 | 2022-04-26 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene |
| CN114870909A (en) * | 2022-05-05 | 2022-08-09 | 中国石油化工股份有限公司 | Method for regenerating catalytic cracking spent catalyst |
| CN115805046A (en) * | 2021-09-15 | 2023-03-17 | 中国石油天然气股份有限公司 | Gas phase ultra-stable reactor, device and method for improving silicon-aluminum ratio of catalytic cracking catalyst |
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| CN104549565A (en) * | 2013-10-17 | 2015-04-29 | 中国石油化工股份有限公司 | Regenerator for catalytic conversion and regeneration method |
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| US11084765B2 (en) | 2017-04-27 | 2021-08-10 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene |
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| WO2018196361A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Fluidized bed apparatus and method for preparing para-xylene co-produced low-carbon olefin from methanol and/or dimethyl ether and toluene |
| CN113231109A (en) * | 2021-04-25 | 2021-08-10 | 西安航天源动力工程有限公司 | Waste catalyst regeneration reaction furnace |
| CN115805046A (en) * | 2021-09-15 | 2023-03-17 | 中国石油天然气股份有限公司 | Gas phase ultra-stable reactor, device and method for improving silicon-aluminum ratio of catalytic cracking catalyst |
| CN114870909A (en) * | 2022-05-05 | 2022-08-09 | 中国石油化工股份有限公司 | Method for regenerating catalytic cracking spent catalyst |
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