CN104549565A - Regenerator for catalytic conversion and regeneration method - Google Patents
Regenerator for catalytic conversion and regeneration method Download PDFInfo
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Abstract
A regenerator for catalytic conversion comprises a regeneration zone, a delivery pipe, gas-solid separation equipment and a flue gas collection chamber, wherein one end of the delivery pipe is communicated with the regeneration zone, the other end of the delivery pipe is communicated with the gas-solid separation equipment in an airtight manner, the gas-solid separation equipment is located outside the regeneration zone, a material leg of the gas-solid separation equipment extends into the regeneration zone, and a gas rising pipe of the gas-solid separation equipment is communicated with the flue gas collection chamber. A spent catalyst enters the regeneration zone and is burnt in the presence of a regeneration medium, and a regenerated catalyst leaves the regeneration zone; regeneration flue gas coming from the regeneration zone and the carried catalyst enter the gas-solid separation equipment via the delivery pipe, the flue gas separated by the gas-solid separation equipment enters the flue gas collection chamber and is discharged by a regeneration flue gas delivery pipe. According to the regenerator, gas-solid separators are arranged outside the regenerator, so that damage caused by high temperatures of the regeneration zone and tail combustion to the gas-solid separators is reduced; a settling section can be omitted, so that the height of the regenerator is decreased; after three stages of gas-solid separators are adopted, the gas-solid separation effect is substantially improved.
Description
Technical field
The present invention relates to the regenerator and renovation process that burn containing Pd/carbon catalyst in catalytic cracking process.
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 development 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 %, and coke burning degree is low, is about 100kg(amount of coke)/[the 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, first paragraph regeneration is upper, the temperature of first paragraph is 650 ~ 720 DEG C, second segment regeneration under, the temperature of second segment regenerator is 650 ~ 780 DEG C, is connected as a single entity between two regenerators with the distribution grid of low pressure drop, 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.
At present, the effect of regenerator dilute phase section is except for placing the equipment such as gas solid separation system, another one important function is just to provide certain space, the catalyst granules bringing dilute phase into is as often as possible settled down by the effect of the gravity of particle own, returns dense-phase bed.Thus make regenerated flue gas bring the catalyst sedimentation of cyclone separator into minimum level, to reduce the solid loading of cyclone separator, reduce the loss of catalyst, therefore regenerator dilute phase section is also sometimes referred to as settler.The height of dilute phase section needs usually higher than transportation deposit height, after exceeding this height, carries amount of solid and does not substantially decline in continuation.Because dilute phase section linear speed is higher, required transportation deposit height is higher, and therefore, dilute phase section diameter must can not be less than close phase section diameter.In actual production, owing to arranging equipment in settler, dilute phase section is highly about 1.8 ~ 2.0 times of transportation deposit height, thus causes device height to increase.
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, can effectively reduce device height, reduce exhanst gas outlet dust concentration.
A kind of regenerator for catalyzed conversion provided by the invention, it is characterized in that this regenerator comprises renewing zone, carrier pipe, gas-solid separation equipment, flue gas collection chamber, wherein one end of carrier pipe is communicated with renewing zone, the other end of carrier pipe is communicated with gas-solid separation equipment is airtight, gas-solid separation equipment is positioned at outside renewing zone, the dipleg of gas-solid separation equipment stretches in renewing zone, and the riser of gas-solid separation equipment is communicated with flue gas collection chamber.
In some embodiments of regenerator of the present invention, described renewing zone is 1-2 dense-phase fluidized bed.
In some embodiments of regenerator of the present invention, described renewing zone is 1-2 fast fluidized bed.
In some embodiments of regenerator of the present invention, described renewing zone is dense-phase fluidized bed and fast fluidized bed.
In some embodiments of regenerator of the present invention, described gas-solid separation equipment is 1-3 cyclone separator, a preferred 2-3 cyclone separator.
In some embodiments of regenerator of the present invention, described cyclone separator series connection.
In some embodiments of regenerator of the present invention, described first cyclone separator is connected by flue gas distributing pipe with between second cyclone separator.
In some embodiments of regenerator of the present invention, described renewing zone is provided with regenerating medium entrance, reclaimable catalyst entrance and regenerated catalyst outlet.
In some embodiments of regenerator of the present invention, described flue gas collection chamber is connected with regenerated flue gas feed-line.
A kind of renovation process for catalyzed conversion provided by the invention, is characterized in that the method comprises the following steps:
(1), reclaimable catalyst enters renewing zone, and burn under regenerating medium exists, regenerated catalyst leaves renewing zone;
(2) regenerated flue gas, from renewing zone enters gas-solid separation equipment with the catalyst carried through carrier pipe;
(3) flue gas, be separated from gas-solid separation equipment enters flue gas collection chamber and discharges through regenerated flue gas feed-line.
In some embodiments of renovation process of the present invention, described gas-solid separation equipment is positioned at outside renewing zone, and the dipleg of gas-solid separation equipment stretches in renewing zone.
In some embodiments of renovation process of the present invention, described gas-solid separation equipment is 1-3 cyclone separator, a preferred 2-3 cyclone separator.
In some embodiments of renovation process of the present invention, described cyclone separator series connection.
In some embodiments of renovation process of the present invention, described first cyclone separator is connected by flue gas distributing pipe with between second cyclone separator.
The regeneration temperature of the renewing zone of renovation process of the present invention is 600 ~ 900 DEG C preferably 650 ~ 750 DEG C, and gas superficial linear velocity is 0.2 ~ 10.0 meter per second preferably 0.3 ~ 3.0 meter per second.
The invention has the advantages that:
1, gas-solid separator can be arranged on outside regenerator, reduces renewing zone high temperature and the infringement of tail combustion to gas-solid separator.
2, regenerator also can not establish settling section, and regenerator height is reduced.
3, after adopting three grades of gas-solid separators, gas-solid separating effect significantly improves.
Accompanying drawing explanation
The basic equipment schematic diagram of Fig. 1,2,3,4 for being embodiment 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.
Fig. 1 equipment comprises dense-phase fluidized bed renewing zone 1, carrier pipe 2, the first gas-solid separator 3, second gas-solid separator 4,3rd gas-solid separator 5, dipleg 6,7 and 9, flutter valve 8 and 10, flue gas collection chamber 11, main air pipeline 12, reclaimable catalyst feed-line 13, main air distributor 14, regenerated catalyst line 15, flue gas delivery pipe line 16.
As shown in Figure 1, reclaimable catalyst enters renewing zone 1 through pipeline 13, regenerate with regeneration gas 12 counter current contacting after distributing through main air distributor 14, regenerated flue gas and the catalyst dust carried thereof enter carrier pipe 2, enter first order gas-solid separator 3, catalyst after first order gas-solid separator is separated and the flue gas carried thereof return to renewing zone 1 through dipleg 6, flue gas after first order gas-solid separator is separated and the catalyst dust carried thereof enter second level gas-solid separator 4, catalyst after second level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 7, flutter valve 8 returns to renewing zone 1, flue gas after second level gas-solid separator is separated and the catalyst dust carried thereof enter third level gas-solid separator 5, catalyst after third level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 9, flutter valve 10 returns to renewing zone 1, flue gas after third level gas-solid separator is separated and the trace catalyst dust carried thereof enter flue gas collection chamber 11, follow-up flue gas processing device (not indicating in figure) is sent into through pipeline 16.
Embodiment two:
Fig. 2 is the basic equipment schematic diagram of embodiment two provided by the invention.
Fig. 2 equipment comprises dense-phase fluidized bed renewing zone 1, carrier pipe 2, the first gas-solid separator 3, second gas-solid separator the 4, three gas-solid separator 5, dipleg 6,7 and 9, flutter valve 8 and 10, flue gas collection chamber 11, main air pipeline 12, reclaimable catalyst feed-line 13, fast fluidized bed renewing zone 14, regenerated catalyst line 15, flue gas delivery pipe line 16, heat collector 17, regenerated catalyst pipeloop 18.
As shown in Figure 2, reclaimable catalyst enters renewing zone 14 through pipeline 13, contact with regeneration gas 12 and regenerate, regenerated flue gas and the catalyst dust carried thereof enter renewing zone 1, part thermocatalyst returns to renewing zone 14 through pipeloop 18, and part hot regenerated catalyst enters renewing zone 14 after heat collector 17 heat-obtaining.Partial regeneration catalyst is sent to reactor (not indicating in figure) through pipeline 15.Regenerated flue gas in renewing zone 1 and the catalyst dust carrier pipe 2 carried thereof, enter first order gas-solid separator 3, catalyst after first order gas-solid separator is separated and the flue gas carried thereof return to renewing zone 1 through dipleg 6, flue gas after first order gas-solid separator is separated and the catalyst dust carried thereof enter second level gas-solid separator 4, catalyst after second level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 7, flutter valve 8 returns to renewing zone 1, flue gas after second level gas-solid separator is separated and the catalyst dust carried thereof enter third level gas-solid separator 5, catalyst after third level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 9, flutter valve 10 returns to renewing zone 1, flue gas after third level gas-solid separator is separated and the trace catalyst dust carried thereof enter flue gas collection chamber 11, follow-up flue gas processing device (not indicating in figure) is sent into through pipeline 16.
Embodiment three:
Fig. 3 is the basic equipment schematic diagram of embodiment three provided by the invention.
Fig. 3 equipment comprises dense-phase fluidized bed renewing zone 1, carrier pipe 2, the first gas-solid separator 3, second gas-solid separator 4,3rd gas-solid separator 5, dipleg 6,7 and 9, flutter valve 8 and 10, flue gas collection chamber 11, main air pipeline 12, reclaimable catalyst feed-line 13, dense-phase fluidized bed renewing zone 14, regenerated catalyst line 15, flue gas delivery pipe line 16.
As shown in Figure 3, reclaimable catalyst enters renewing zone 14 through pipeline 13, contact with regeneration gas 12 and regenerate, regenerated flue gas and the catalyst dust carried thereof enter renewing zone 1, part thermocatalyst returns to renewing zone 14 through pipeloop (not indicating in figure), and part hot regenerated catalyst enters renewing zone 14 after heat collector (not indicating in figure) heat-obtaining.Partial regeneration catalyst is sent to reactor (not indicating in figure) through pipeline 15.Regenerated flue gas in renewing zone 1 and the catalyst dust carrier pipe 2 carried thereof, enter first order gas-solid separator 3, catalyst after first order gas-solid separator is separated and the flue gas carried thereof return to renewing zone 1 through dipleg 6, flue gas after first order gas-solid separator is separated and the catalyst dust carried thereof enter second level gas-solid separator 4, catalyst after second level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 7, flutter valve 8 returns to renewing zone 1, flue gas after second level gas-solid separator is separated and the catalyst dust carried thereof enter third level gas-solid separator 5, catalyst after third level gas-solid separator is separated and the flue gas that carries thereof are through dipleg 9, flutter valve 10 returns to renewing zone 1, flue gas after third level gas-solid separator is separated and the trace catalyst dust carried thereof enter flue gas collection chamber 11, follow-up flue gas processing device (not indicating in figure) is sent into through pipeline 16.
Embodiment four:
Fig. 4 is the basic equipment schematic diagram of embodiment four provided by the invention.
Fig. 4 equipment comprises carrier pipe 2, the first gas-solid separator 3, second gas-solid separator 4, flue gas distributing pipe 19, flue gas collection chamber 11, flue gas delivery pipe line 16.
As shown in Figure 4, vertical tranporter 2 is entered from the regenerated flue gas of renewing zone (not indicating in figure) and the catalyst dust that carries thereof, enter first order gas-solid separator 3, catalyst after first order gas-solid separator is separated and the flue gas carried thereof return to renewing zone, flue gas after first order gas-solid separator is separated and the catalyst dust carried thereof enter flue gas distributing pipe 19, in flue gas distributing pipe, flue gas enters second level gas-solid separator 4, catalyst after second level gas-solid separator is separated and the flue gas carried thereof return to renewing zone, flue gas after second level gas-solid separator is separated and the catalyst dust carried thereof enter flue gas collection chamber 11, follow-up flue gas processing device (not indicating in figure) is sent into through pipeline 16.
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) (slag gas oil mixed in abbreviation) 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 1.Regenerate according to regenerator proposed by the invention, gas-solid separator is cyclone separator, and regeneration gas is air, the prevailing operating conditions of regenerator and the results are shown in Table 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 |
| The KK(end point of distillation) | 520 |
Table 2
| Embodiment 1 | |
| Bed gas superficial velocity, meter per second | 0.9 |
| Regeneration temperature, DEG C | 700 |
| First order cyclone inlet linear speed, meter per second | 19 |
| Regenerated catalyst carbon content, heavy % | 0.06 |
| Dust Capacity (wet basis) in flue gas, milligram/cubic meter | 102 |
Claims (18)
1. the regenerator for catalyzed conversion, it is characterized in that this regenerator comprises renewing zone, carrier pipe, gas-solid separation equipment, flue gas collection chamber, wherein one end of carrier pipe is communicated with renewing zone, the other end of carrier pipe is communicated with gas-solid separation equipment is airtight, gas-solid separation equipment is positioned at outside renewing zone, the dipleg of gas-solid separation equipment stretches in renewing zone, and the riser of gas-solid separation equipment is communicated with flue gas collection chamber.
2., according to regenerator according to claim 1, it is characterized in that described renewing zone is 1-3 dense-phase fluidized bed.
3., according to regenerator according to claim 1, it is characterized in that described renewing zone is 1-2 fast fluidized bed.
4., according to regenerator according to claim 1, it is characterized in that described renewing zone is dense-phase fluidized bed and fast fluidized bed.
5., according to regenerator according to claim 1, it is characterized in that described gas-solid separation equipment is 1-3 cyclone separator.
6., according to regenerator according to claim 5, it is characterized in that described gas-solid separation equipment is 2-3 cyclone separator.
7., according to regenerator according to claim 6, it is characterized in that described cyclone separator is connected.
8., according to regenerator according to claim 6, it is characterized in that described first cyclone separator is connected by flue gas distributing pipe with between second cyclone separator.
9., according to regenerator according to claim 1, it is characterized in that described renewing zone is provided with regenerating medium entrance, reclaimable catalyst entrance and regenerated catalyst outlet.
10., according to regenerator according to claim 1, it is characterized in that described flue gas collection chamber is connected with regenerated flue gas feed-line.
11. 1 kinds of renovation process for catalyzed conversion, is characterized in that the method comprises the following steps:
(1), reclaimable catalyst enters renewing zone, and burn under regenerating medium exists, regenerated catalyst leaves renewing zone;
(2) regenerated flue gas, from renewing zone enters gas-solid separation equipment with the catalyst carried through carrier pipe;
(3) flue gas, be separated from gas-solid separation equipment enters flue gas collection chamber and discharges through regenerated flue gas feed-line.
12. in accordance with the method for claim 11, and it is characterized in that described gas-solid separation equipment is positioned at outside renewing zone, the dipleg of gas-solid separation equipment stretches in renewing zone.
13. in accordance with the method for claim 11, it is characterized in that described gas-solid separation equipment is 1-3 cyclone separator.
14. in accordance with the method for claim 11, it is characterized in that described gas-solid separation equipment is 2-3 cyclone separator.
15. in accordance with the method for claim 14, it is characterized in that described cyclone separator is connected.
16. in accordance with the method for claim 14, it is characterized in that described first cyclone separator is connected by flue gas distributing pipe with between second cyclone separator.
17. in accordance with the method for claim 11, and it is characterized in that the regeneration temperature of described renewing zone is 600 ~ 900 DEG C, gas superficial linear velocity is 0.2 ~ 10.0 meter per second.
18. in accordance with the method for claim 17, and it is characterized in that the regeneration temperature of described renewing zone is 650 ~ 750 DEG C, gas superficial linear velocity is 0.3 ~ 3.0 meter per second.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107011940A (en) * | 2016-01-28 | 2017-08-04 | 中国石油天然气集团公司 | Catalytic cracking unit |
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| CN103055961A (en) * | 2011-10-19 | 2013-04-24 | 中国石油化工股份有限公司 | Catalyst regeneration method with characteristic of emission reduction |
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| EP0324286A1 (en) * | 1987-12-30 | 1989-07-19 | Mobil Oil Corporation | Improved high efficiency regenerator apparatus |
| CN101171082A (en) * | 2005-04-29 | 2008-04-30 | 格雷斯公司 | NOx reduction compositions for use in partial burn FCC processes |
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