CN103028449B - catalytic conversion catalyst regenerator - Google Patents
catalytic conversion catalyst regenerator Download PDFInfo
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- CN103028449B CN103028449B CN201110291029.6A CN201110291029A CN103028449B CN 103028449 B CN103028449 B CN 103028449B CN 201110291029 A CN201110291029 A CN 201110291029A CN 103028449 B CN103028449 B CN 103028449B
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Abstract
Catalytic conversion catalyst regenerator, comprise renewing zone, decanting zone, buffering area and optional cooling area, wherein said buffering area is adjacent with described renewing zone, buffering area is provided with catalyst inlet and catalyst outlet, wherein catalyst inlet is with cooling area or/and inclined tube to be generated is connected, and is preferably connected with cooling area; Catalyst outlet is connected with regenerator sloped tube; Catalytic conversion catalyst regeneration method comprises reclaimable catalyst and enters regenerator renewing zone, and contact with oxygen-containing gas and combustion reaction occurs, gained regenerated catalyst enters buffering area, and regenerated catalyst is Returning reactor after cooling, and flue gas is discharged from top, decanting zone.The present invention adopts buffering area, and catalyst temperature is evenly distributed, and has cooling-down effect for regenerator dilute phase, is not easy to occur dilute phase overheating problem.
Description
Technical field
The present invention relates in catalytic cracking process containing the regenerator that Pd/carbon catalyst burns.
Background technology
Feedstock oil, while carrying out catalytic cracking reaction, owing to there is condensation reaction, except generation light hydrocarbons, also generates a part of coke, deposits on a catalyst thus the activity and selectivity of catalyst is reduced.Therefore, adopt high-temperature oxydation renovation process, the serviceability recovering catalyst is removed in the coke burning on catalyst, and this process is called the regeneration of catalyst, usually the catalyst of deposit coke is called reclaimable catalyst, the catalyst after oxidation regeneration is called regenerated catalyst.Burning process completes in regenerator, can be divided into turbulent bed, fast bed and conveying bed etc. according to regenerator fluid bed type difference; Burning and partial combustion completely can be divided into according to CO burning degree; According to catalyst different with Air for burning coke flow process can be divided into and flow, cross-flow and adverse current burn; Single hop and two-stage regeneration can be divided into according to burning fluidized bed region difference; Single device, two devices and many devices can be divided into burn according to the difference of scorched area container.Catalytic cracking regenerator generally comprises for the regeneration function district of reclaimable catalyst regeneration, for settled catalyst and the sedimentation function district of placing gas-solid separator, along with the propelling of RFCC, regenerator adds the cooling function district with catalyst heat-obtaining function.
Early stage catalyst recovery process passes into oxygen-containing gas in low speed circulating fluidized bed, and adopt single hop regeneration, in the fluid bed of this low linear speed, the full back-mixing of gas-solid, gas and solid contact efficiency low, catalyst regeneration speed is slow, result in regenerator catalyst reserve excessive, the regeneration effect of catalyst is poor, regenerated catalyst carbon content is about 0.2 heavy %, coke burning degree is low, is about 100kg (amount of coke)/[h (unit interval) T (catalyst inventory)].Along with molecular sieve catalyst uses widely on catalytic cracking unit, the especially use of the molecular sieve catalyst of USY type, carbon content remaining on regenerated catalyst and regeneration very large on the activity and selective impact of recovering catalyst.Therefore, effectively to reduce in regenerative process catalyst inventory and improve the direction that catalyst regeneration effect becomes regeneration techniques exploitation.This is because in catalytic cracking unit runs, catalyst is constantly subject to the effect of high temperature and water vapour, the heavy metal deposition carried in feedstock oil is on catalyst surface, the activity of catalyst constantly reduces, need fresh makeup catalyst to maintain the equilibrium activity of catalyst in reaction-regeneration system, when fresh catalyst magnitude of recruitment one timing, in reaction-regeneration system, catalyst general reserve is lower, catalyst replacement rate is higher, and so the equilibrium activity of reaction-regeneration system catalyst is also higher.
USP3563911 discloses a kind of two-stage regeneration, reclaimable catalyst sequentially passes through the first dense-phase fluidized bed and the second dense-phase fluidized bed, contact with oxygen containing gas and make coke generation combustion reaction on catalyst surface, the flue gas produced mixing also entrained catalyst enters dilute phase settling section.First dense-phase fluidized bed regeneration temperature is greater than 1050 °F (namely 565.5 DEG C); The gas superficial linear velocity of the second dense-phase fluidized bed is 1.25 feet per second ~ 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 DEG C).The method is compared with catalyst single hop renovation process, and under the condition that regenerative process carbon-burning load is not high, the reserve of regenerator inner catalyst can reduce nearly 40%, and the carbon content of regenerated catalyst can 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, catalyst mean residence time is 0.6 ~ 1.0 minute, and regeneration temperature is 650 ~ 750 DEG C; After catalyst removes most of coke in the first fluidized bed, the catalyst of partial regeneration is together with gas and stream is upward through distributor, enter the second fluid bed, the combustion reaction of concurrent green coke charcoal is contacted again with oxygen containing gas, the gas superficial linear velocity of the second dense-phase fluidized bed is 1.2 ~ 3.0 meter per seconds, catalyst mean residence time is 1.0 ~ 2.2 minutes, regeneration temperature is 700 ~ 800 DEG C, after catalyst is fully regenerated, regenerated catalyst is separated 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 of regeneration is upper, the temperature of first paragraph is 650 ~ 720 DEG C, two sections regeneration under, the temperature of second segment regenerator is 650 ~ 780 DEG C, is connected as a single entity between two regenerators with low pressure drop distribution grid, and two regenerators only need with a flue and a double slide valve or butterfly valve.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 comparing mitigation and abrasive conditions always, regenerated catalyst carbon content is controlled below 0.10 % by weight, be preferably lower than 0.05 % by weight, coke burning degree brings up to more than 100kg/ (th), reach the highest to realize regenerated catalyst activation recovering, thus the conversion capability realizing hydro carbons is maximum.Therefore, after adopting highly active zeolite catalyst, regenerator superficial gas flow velocity increases to more than 0.6 meter per second, coke burning degree brings up to more than 100kg/ (th), catalyst residence times is less than 4 minutes, and regeneration temperature needs to remain enough high and burns temperature, burns dynamics to improve.But very important is when regeneration temperature height, regenerated catalyst and feedstock oil first contacts temperature improve thereupon, easily there is the problem that dry gas and coke yield increase, in addition because regenerated catalyst temperature is higher, therefore the oil ratio of corresponding catalytic cracking unit declines thereupon, and heavy oil conversion performance is deteriorated.In order to alleviate this contradiction, cooling catalyst technology is paid close attention to gradually.
US3679576 discloses a kind of fluid catalytic cracker and technique, and this technique reaches by reclaimable catalyst and regenerated catalyst mixing the object reducing catalyst temperature, thus reaches increase conversion ratio, reduces the object of dry gas and coke yield.
US5451313 discloses the recirculation reactor of catalytically cracked material and catalyst exposure, first this reactor allows the reclaimable catalyst from reactor stripper and the regenerated catalyst from regenerator mix being positioned at the mixed zone bottom catalytic cracking unit riser, reach the object reducing catalyst temperature, then the catalyst after cooling contacts with feedstock oil and carries out catalyzed conversion, thus reaches the object increasing conversion ratio and reduce dry gas and coke.
CN101665713A provides a kind of round-robin method and equipment thereof of cold regenerated catalyst, from regenerator regenerated catalyst through catalyst cooler be cooled to 200 DEG C ~ 720 DEG C not with or enter riser reactor after mixing without the hot regenerated catalyst cooled with another part, hydrocarbon raw material reacts at riser reactor and catalyst exposure, thus reaches the object increasing conversion ratio and reduce dry gas and coke.
CN101191071A and CN101191072A provides the regenerated catalyst thermoregulation equipment of catalytic cracking unit, its main method is that regenerated catalyst is introduced cooling catalyst district, heat-obtaining is carried out by heat collector in cooling area, then the catalyst after cooling contacts with feedstock oil and carries out catalyzed conversion, thus reaches the object increasing 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 outlet port and hot regenerated catalyst outlet port, cooling catalyst device is connected with regenerator dense bed by catalyst outlet port, the pre-lift blender being arranged on riser reactor conversion zone bottom is connected with cooling catalyst device with cold renewal guiding valve by cold regenerated catalyst carrier pipe, is connected with hot recycling guiding valve by hot regenerated catalyst carrier pipe with regenerator dense bed.The method can make the oil ratio in catalytic cracking reaction process improve flexibly.
The appearance of Novel cold thermocatalyst hybrid cooling functional areas, achieves the object that catalytic cracking unit improves product slates to a certain extent.But when needing the internal circulating load increasing substantially catalyst, existing catalyst mix falling temperature technique cannot stably for riser reactor provides even heat and the uniform catalyst of fluidisation.For complete combustion system, when carbon monoxide close mutually in completely burning rise to dilute phase burning there will be tail combustion phenomenon, occur reason mainly comprises main air skewness, catalyst fluidization is bad, dense-phase bed is too low, fresh catalyst supplement too fast, combustion adjuvant is not enough, external warmer return catalizer detours, after there is tail combustion, dilute phase temperature often rises rapidly, close to or more than 800 DEG C, thus make regenerator overtemperature.Regenerator overtemperature can damage equipment in settler, inner member and lining, causes pressure oscillation, can affect device even running if dealt with improperly.If adopt platinum based carbon monoxide combustion adjuvant, catalytic cracking unit NOx emission can be caused to increase due to the catalytic action of platinum.
Summary of the invention
The object of the invention is to provide a kind of Catalytic conversion catalyst regenerator on the basis of existing technology, to prevent regenerator overtemperature, stably for riser reactor provides lower temperature and the catalyst of even heat.
Catalytic conversion 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.Renewing zone can be established one or more.Renewing zone is provided with catalyst inlet and catalyst outlet, and wherein catalyst inlet is connected with inclined tube to be generated, and catalyst outlet, is preferably connected with cooling area or/and regenerated catalyst pipe is connected with cooling area.One or more catalyst dispenser is set in renewing zone for distributing catalyst, one or more main air distributor is also set in renewing zone as distribution grid or distributor pipe, for the oxygen-containing gas that distributes (also referred to as main air).
Described decanting zone is for catalyst sedimentation or/and place gas-solid separation equipment functional area, and catalyst is gas phase fluidization state in this district, and Ye Chenggai district is dilute-phase zone, and exhanst gas outlet is established at top, decanting zone.When each district of regenerator is arranged vertically, generally 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 is with cooling area or/and inclined tube to be generated is connected, and is preferably connected with cooling area; Catalyst outlet is connected with regenerator sloped tube.
Described buffering area is adjacent with described renewing zone.When each district of regenerator is arranged vertically, the position of buffering area can be arranged flexibly, both can below renewing zone, also can on renewing zone, also can in the middle of multiple renewing zone.One or more catalyst dispenser is set in buffering area for distributing catalyst, one or more fluidizing agent distributor is also set in buffering area for the fluidizing agent that distributes.
Described cooling area reduces temperature function district for high temperature catalyst, and regenerator can arrange cooling area, also can not arrange cooling area, preferably arrange cooling area.Cooling area is located between buffering area and renewing zone.In cooling area, adopt the mode of heat collector to carry out heat-obtaining cooling to catalyst.
Renewing zone, decanting zone, buffering area and optional cooling area can arrange multiple, such as, can arrange one or more renewing zone, also can arrange cooling area or multiple cooling areas etc.Can be connected to each other directly for identical function district, also can not directly connect.
The connected mode of renewing zone, decanting zone, buffering area and optional cooling area is selected from that wall is connected, tubular type connection, board-like connection, one or more in gas-solid separator connection, wherein tubular type connection is selected from one or more in the connection of dilute phase pipe, distributor pipe connection, carrier pipe connection, T-shaped pipe, board-like connection preferred distribution plate connects, and gas-solid separator connects preferred cyclone separator or/and thick cyclone separator.
Catalytic conversion catalyst regeneration method provided by the invention comprises: reclaimable catalyst enters regenerator renewing zone, contact with oxygen-containing gas and combustion reaction occurs, gained regenerated catalyst enters buffering area, and regenerated catalyst is Returning reactor after cooling, and flue gas is discharged from top, decanting zone.
In renewing zone, described catalyst mean residence time is 0.5 ~ 30 minute, is preferably 1.5 ~ 10 minutes; Described temperature is 600 ~ 900 DEG C, is preferably 650 ~ 750 DEG C; Described gas superficial linear velocity is 0.2 ~ 5.0 meter per second, is preferably 0.5 ~ 3.5 meter per second; 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 DEG C, is preferably 500 ~ 680 DEG C; Described gas superficial linear velocity is 0.1 ~ 4.0 meter per second, is preferably 0.2 ~ 0.9 meter per second.
Buffering area fluidizing agent is selected from one or more in inert gas, oxidizing gas, reducibility gas, wherein inert gas is that steam is or/and carbon dioxide containing gas, oxidizing gas be air or/and oxygen-containing gas, reducibility gas is selected from dry gas, containing one or more in CO gas, flue gas.
Buffering area catalyst is selected from one or more in cooling area, renewing zone, stripping rear catalyst.
In renewing zone, adopt regeneration to be selected from holomorphosis mode, incomplete regen-eration mode one or more.
The invention has the advantages that:
1, buffering area catalyst temperature is evenly distributed, and separate sources catalyst mix is even.
2, the heavy metal on catalyst surface is under low temperature and long-time operation condition, and part heavy metal is buried by matrix, and remaining part heavy metal is passivated.
3, buffering area has cooling-down effect for regenerator dilute phase, is not easy to occur dilute phase overheating problem.
Accompanying drawing explanation
The basic equipment schematic diagram of Fig. 1,2,3,4,5 for being five kinds of embodiments provided by the invention.
Detailed description of the invention
Further illustrate 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 buffering area 1, and renewing zone 3 is single hop regeneration, and renewing zone 2 and decanting zone 4 adopt the direct-connected mode of wall.The reclaimable catalyst carrying out autoreactor enters renewing zone 2 through inclined tube 6 to be generated and is uniformly distributed in dense bed top through distributor, main air to be entered from the bottom of renewing zone 2 by main air distributing plate 10 through pipeline 11 and upwards flows, with the reclaimable catalyst counter current contacting concurrent green coke charcoal combustion reaction flowed downward by gravity, catalyst activity is restored, flue gas is successively through decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating in figure), part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collector, fluidizing agent 13 to enter from the bottom of buffering area 1 through fluidizing agent distributor 12 and carries out fluidisation to cooling rear catalyst, fluidizing agent gas in buffering area 1 enters decanting zone 4 through balance pipe 16, regenerated catalyst in buffering area 1 enters riser reactor through regenerator sloped tube 7 and to contact with feedstock oil catalytic cracking reaction (not indicating in figure) occurs.
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 in renewing zone 2, between renewing zone 3 and buffering area 1, renewing zone 2 and 3 is band burning tank regeneration, and renewing zone 3 and decanting zone 4 adopt the direct-connected mode of wall.The reclaimable catalyst carrying out autoreactor enters through inclined tube 6 to be generated and burns the high temperature catalyst returned with circulation pipe 14 bottom pot type renewing zone 2 and mix 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, mixing rear catalyst with oxygen-containing gas with fast bed form upwards, oxygen-containing gas contacts the combustion reaction of concurrent green coke charcoal with mixed catalyst at relatively high temperatures, be restored close to more than 80% catalyst activity, semi regeneration catalyst and flue gas are successively through dilute phase pipe, semi regeneration catalyst is separated with flue gas (not indicating in figure) by thick cyclone separator, catalyst falls into renewing zone 3 dense-phase bed, oxygen-containing gas is sent in dense-phase bed, semi regeneration catalyst is made to be in fluidized state and to proceed coke burning regeneration, in the dense-phase bed of renewing zone 3, a part of high temperature catalyst returns in the burning tank of renewing zone 2 through circulation pipe 14 and provides heat, flue gas is through decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating in figure), part regenerated catalyst enters buffering area 1 after cooling area 5 lowers the temperature, the bottom that fluidizing agent 13 enters buffering area 1 through fluidizing agent distributor 12 makes cooling catalyst be in fluidized state, in buffering area 1, fluidizing agent gas enters decanting zone 4 through balance pipe 16, in buffering area 1, a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and to contact with feedstock oil catalytic cracking reaction (not indicating in figure) occurs.
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 buffering area 1, and renewing zone 2 is single hop regeneration, and buffering area 1 and decanting zone 4 adopt the direct-connected mode of wall.The reclaimable catalyst carrying out autoreactor enters renewing zone 2 through inclined tube 6 to be generated and is uniformly distributed in dense bed top through distributor, main air to be entered from the bottom of renewing zone 2 by main air distributing plate 10 through pipeline 11 and upwards flows, with the reclaimable catalyst counter current contacting concurrent green coke charcoal combustion reaction flowed downward by gravity, catalyst activity is restored, flue gas enters buffering area 1 through wide bore distribution plate 11 and makes buffering area cooling catalyst be in fluidized state, part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collector, high-temperature flue gas through buffering area 1 lower the temperature catalyst cooling after successively through decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating in figure), in buffering area 1, a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and to contact with feedstock oil catalytic cracking reaction (not indicating in figure) occurs, another part regenerated catalyst returns to renewing zone 2 for controlling regeneration temperature through regenerated catalyst pipe 14.
Embodiment four:
Fig. 4 is substantially putting for schematic diagram 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 buffering area 1, and renewing zone 2 and renewing zone 3 are two-stage regeneration mode, and buffering area 1 and decanting zone 4 adopt the direct-connected mode of wall.The reclaimable catalyst carrying out autoreactor enters turbulent bed renewing zone 2 through inclined tube 6 to be generated and is uniformly distributed in through distributor oxygen-containing gas dense bed top and bottom sent into and carries out oxygen deprivation regeneration, high-temperature flue gas through buffering area 1 lower the temperature catalyst cooling after successively through decanting zone 4, cyclone separator 8, flue gas pipeline 9 enters smoke energy recovering system (not indicating in figure), semi regeneration catalyst is drawn from bottom, renewing zone 2, turbulent bed renewing zone 3 is entered through semi regeneration catalyst tube 15, main air to be entered from the bottom of renewing zone 3 by main air distributing plate 10 through pipeline 11 and carries out oxygen enrichment regeneration, the remaining coke of burning-off, catalyst activity is restored, renewing zone 3 flue gas enters renewing zone 2 through top wide bore distribution plate (not indicating in figure), excess oxygen in flue gas continues to burn utilization in renewing zone 2, part high-temperature regenerated catalyst enters buffering area 1 after the cooling of cooling area 5 heat collector, in buffering area 1, a part of regenerated catalyst enters riser reactor through regenerator sloped tube 7 and to contact with feedstock oil catalytic cracking reaction (not indicating in figure) occurs.
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 single hop regeneration, and renewing zone 2 and decanting zone 4 adopt the direct-connected mode of wall.The reclaimable catalyst carrying out autoreactor enters renewing zone 2 through inclined tube 6 to be generated and is uniformly distributed in dense bed top through distributor, main air to be entered from the bottom of renewing zone 2 by main air distributing plate 10 through pipeline 11 and upwards flows, with the reclaimable catalyst counter current contacting concurrent green coke charcoal combustion reaction flowed downward by gravity, catalyst activity is restored, flue gas is successively through decanting zone 4, cyclone separator 8 and flue gas pipeline 9 enter smoke energy recovering system (not indicating in 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 to enter from the bottom of buffering area 1 through fluidizing agent distributor 12 and carries out fluidisation to mixed catalyst, in buffering area 1, fluidizing agent gas enters renewing zone 2 through dilute phase pipe 18, in buffering area 1, a part of mixed catalyst enters riser reactor through regenerator sloped tube 7 and to contact with feedstock oil catalytic cracking reaction (not indicating in figure) occurs.
The following examples will be further described the present invention, but not thereby limiting the invention.The feedstock oil used in embodiment and comparative example is the vacuum gas oil (VGO) (mixing slag gas oil) mixing decompression residuum, and its character lists in table 1.Catalyst is produced by catalyst branch company of Sinopec Group, and goods number is CGP-1.
Embodiment 1
The present embodiment carries out on kitty cracker, as shown in Figure 3.Regenerate according to regenerator proposed by the invention, namely renewing zone is adverse current single hop regeneration, and heat-obtaining rear catalyst enters buffering area, the prevailing operating conditions of regenerator and the results are shown in Table 2.
Comparative example 1
Comparative example 1 is also carry out on the kitty cracker identical with embodiment 1, the adverse current single hop renovation process pair reclaimable catalyst identical with embodiment routinely regenerates, when adopting comparative example, tail combustion problem is easily there is when regeneration temperature brings up to 650 ~ 680 DEG C, for quiet run, cannot continue to improve regeneration temperature, regenerator prevailing operating conditions and the results are shown in Table 2.
As can be seen from Table 2, compared with comparative example 1, because the present invention adopts buffering area, make regenerator tail fire phenomenon to be resolved, renewing zone of the present invention regeneration temperature significantly improves, reach 700 DEG C, catalyst burn efficiency be improved significantly, on catalyst, carbon content can reach 0.06 heavy %, be delivered to reactor catalyst temperature and can be reduced to 660 DEG C as required, under the condition that riser reactor raw material preheating temperature is identical with oil ratio, outlet temperature of riser can be reduced to 505 DEG C from 515 of comparative example 1 DEG C.
Embodiment 2
The present embodiment carries out on kitty cracker, as shown in Figure 3.Regenerate according to regenerator proposed by the invention, namely renewing zone is adverse current single hop regeneration, and heat-obtaining rear catalyst and part reclaimable catalyst enter buffering area mixing, the prevailing operating conditions of regenerator and the results are shown in Table 3.
Comparative example 2
Comparative example 2 is also carry out on the kitty cracker identical with embodiment 2, the adverse current single hop renovation process pair reclaimable catalyst identical with embodiment routinely regenerates, when adopting comparative example 2, tail combustion problem is easily there is when regeneration temperature brings up to 650 ~ 680 DEG C, for quiet run, cannot continue to improve regeneration temperature, regenerator prevailing operating conditions and the results are shown in Table 3.
As can be seen from Table 3, compared with comparative example 2, because the present invention adopts buffering area, make regenerator tail fire phenomenon to be resolved, renewing zone of the present invention regeneration temperature significantly improves, reach 710 DEG C, catalyst burn efficiency be improved significantly, on mixed catalyst, carbon content can control at 0.18 heavy % as required, be delivered to reactor catalyst temperature and can be reduced to 660 DEG C as required, riser reactor is under the condition that fuel oil preheating temperature is identical with outlet temperature, and oil ratio can bring up to 8.0 from 6.0 of comparative example 2.
Table 1
| Feedstock oil title | Mix slag gas oil |
| Density (20 DEG C), kg/m 3 | 906.0 |
| Kinematic viscosity, millimeter 2/ second | |
| 80℃ | 32.45 |
| 100℃ | 12.35 |
| Carbon residue, heavy % | 3.3 |
| Condensation point, DEG C | 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, DEG C | |
| HK (initial boiling point) | 316 |
| 10％ | 354 |
| 30％ | 415 |
| 50％ | 450 |
| 70％ | 493 |
| KK (end point of distillation) | 520 |
Table 2
| Embodiment 1 | Comparative example 1 | |
| Regenerator | ||
| Renewing zone | ||
| Gas superficial velocity, meter per second | 0.9 | 0.9 |
| Catalyst residence times, minute | 5.9 | 5.9 |
| Regeneration dense phase temperature, DEG C | 700 | 680 |
| Buffering area | ||
| Gas superficial velocity, meter per second | 0.4 | / |
| Catalyst residence times, minute | 2.0 | / |
| Catalyst temperature, DEG C | 660 | / |
| Decanting zone | ||
| Dilute phase temperature, DEG C | 671 | 720 |
| Cooling area | ||
| Cooling method | Up flow type external warmer | Downflow system external warmer |
| Be delivered to reactor catalyst | ||
| Carbon content on catalyst, heavy % | 0.06 | 0.20 |
| Catalyst temperature, DEG C | 660 | 680 |
| Reactor | ||
| Fuel oil preheating temperature, DEG C | 330 | 330 |
| Oil ratio, m/m | 4.5 | 4.5 |
| Outlet temperature of riser, DEG C | 505 | 515 |
Table 3
| Embodiment 2 | Comparative example 2 | |
| Regenerator | ||
| Renewing zone | ||
| Gas superficial velocity, meter per second | 0.9 | 0.9 |
| Catalyst residence times, minute | 3.0 | 5.9 |
| Regeneration dense phase temperature, DEG C | 710 | 680 |
| Buffering area | ||
| Gas superficial velocity, meter per second | 0.3 | / |
| Catalyst residence times, minute | 4.0 | / |
| Catalyst temperature, DEG C | 660 | / |
| Decanting zone | ||
| Dilute phase temperature, DEG C | 660 | 720 |
| Cooling area | ||
| Cooling method | Downflow system external warmer | Downflow system external warmer |
| Be delivered to reactor catalyst | ||
| Carbon content on catalyst, heavy % | 0.18 | 0.20 |
| Catalyst temperature, DEG C | 660 | 680 |
| Reactor | ||
| Fuel oil preheating temperature, DEG C | 200 | 200 |
| Oil ratio, m/m | 8.0 | 6.0 |
| Outlet temperature of riser, DEG C | 505 | 505 |
Claims (9)
1. Catalytic conversion catalyst regenerator, it is characterized in that this regenerator comprises renewing zone, decanting zone and buffering area, wherein said buffering area is adjacent with described renewing zone, the one or more fluidizing agent distributor of described setting buffers, buffering area fluidizing agent is selected from one or more in inert gas, reducibility gas.
2. Catalytic conversion catalyst regenerator, it is characterized in that this regenerator comprises renewing zone, decanting zone, buffering area and cooling area, wherein said buffering area is adjacent with described renewing zone, the one or more fluidizing agent distributor of described setting buffers, buffering area fluidizing agent is selected from one or more in inert gas, reducibility gas.
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 with cooling area or/and inclined tube to be generated is connected; Catalyst outlet is connected with regenerator sloped tube.
4., according to the regenerator of claim 3, it is characterized in that the catalyst inlet of described buffering area is connected with cooling area.
5., 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 renewing zone.
6., 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 is connected with inclined tube to be generated, catalyst outlet with cooling area or/and regenerated catalyst pipe is connected.
7., according to the regenerator of claim 6, it is characterized in that described renewing zone catalyst outlet is connected with cooling area.
8., according to the regenerator of claim 7, it is characterized in that the catalyst outlet of described renewing zone is connected with cooling area.
9. according to the regenerator of claim 1 or 2, it is characterized in that described renewing zone, decanting zone, buffering area and optional cooling area connected mode be selected from that wall is connected, tubular type connection, board-like connection, one or more in gas-solid separator connection, wherein tubular type connection is selected from one or more in the connection of dilute phase pipe, distributor pipe connection, carrier pipe connection, T-shaped pipe, board-like connection is that distribution grid connects, and gas-solid separator connects for cyclone separator or/and thick cyclone separator.
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| CN201110291029.6A CN103028449B (en) | 2011-09-30 | 2011-09-30 | catalytic conversion catalyst regenerator |
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| CN201110291029.6A CN103028449B (en) | 2011-09-30 | 2011-09-30 | catalytic conversion catalyst regenerator |
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| CN103028449A CN103028449A (en) | 2013-04-10 |
| CN103028449B true CN103028449B (en) | 2016-03-16 |
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| CN201110291029.6A Active CN103028449B (en) | 2011-09-30 | 2011-09-30 | catalytic conversion catalyst regenerator |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104549565B (en) * | 2013-10-17 | 2017-09-29 | 中国石油化工股份有限公司 | A kind of regenerator and renovation process for catalyzed conversion |
| CN104549566B (en) * | 2013-10-17 | 2017-07-25 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regenerator and renovation process |
| 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 |
| CN108786672B (en) | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by using methanol and/or dimethyl ether and benzene |
| CN108786670B (en) | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
| CN108794291B (en) * | 2017-04-27 | 2020-11-27 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefin by 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 |
| CN114870909B (en) * | 2022-05-05 | 2023-10-20 | 中国石油化工股份有限公司 | Method for regenerating catalytic cracking spent catalyst |
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