CN1065286A - Improved two-stage regeneration for fluid catalytic cracking catalyst - Google Patents
Improved two-stage regeneration for fluid catalytic cracking catalyst Download PDFInfo
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- CN1065286A CN1065286A CN 92103780 CN92103780A CN1065286A CN 1065286 A CN1065286 A CN 1065286A CN 92103780 CN92103780 CN 92103780 CN 92103780 A CN92103780 A CN 92103780A CN 1065286 A CN1065286 A CN 1065286A
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Abstract
The present invention proposes a kind of two-stage regeneration of improved fluidized catalytic cracking catalyst.Characteristics are: first section is adopted coke-burning riser, and second section is adopted wire-speed high-gas turbulent bed.Simplify reclaim equiment and technical process, had the intensity of burning height, few, the active advantages of higher of catalyst inventory.
Description
The invention belongs to the improvement of fluidized catalytic cracking catalyst renovation process.Mink cell focus except that generating light hydrocarbons, also generates coke in the catalytic cracking reaction process, be deposited on the catalyst surface, makes catalyst activity reduction.The general method that adopts oxidation regeneration is burnt the coke on the catalyzer, and to recover activity of such catalysts, this process is called catalyst regeneration.Catalyzer after the regeneration is called regenerated catalyst, and the catalyzer that contains coke is called reclaimable catalyst.Its remaining amount of coke is bigger, more remarkable to molecular sieve and super stable molecular sieve catalyzer especially to recovering the catalyst activity influence.Therefore, the intensifying regenerating process is a domestic and international in recent years problem about company and scientific research and designing unit's R and D.
At present, the patent to the catalyzer two-stage regeneration mainly contains three kinds of patterns:
U.S. Patent number USP3,563,911 disclosed two-phase up-flow regenerations, two-stage regeneration device are coaxial-type, and first section for the low-speed turbulent bed places second section revivifier top, and second section is fast bed.Reclaimable catalyst is earlier through one section, one section with containing the oxygen regeneration gas and two sections regenerated flue gas are regenerated, the catalyzer of partial regeneration enters second section by the outer circulating tube gravity flow, and with single-linkage sliding valve control catalyst internal circulating load.Two sections regenerated flue gas enter energy-recuperation system through one section close phase and dilute phase interflow.Its advantage: second section for fast bed can reduce resistance to mass transfer, temperature higher (718～816 ℃), and oxygen partial pressure is also bigger, can improve to burn intensity, and oxygen also can make full use of in two sections regenerated flue gas.(0.75～0.9m/s), resistance to mass transfer is bigger, and two sections on average to burn intensity low but that shortcoming is one section linear speed is lower.More than 80m, riser tube is very long to reacting-settler top mark height, and equipment is huger, and investment is expensive.
U.S. Patent number USP3,844,973 two-stage regeneration, first section is the preposition jar that burns of fast bed common name, charcoal and most of hydrogen of the advanced one section burning-off 80～90% of reclaimable catalyst, and gas line speed is 0.9～3.0m/s, 677～760 ℃ of regeneration temperatures, catalyzer enters alkene phase transfer lime and continues to burn, and CO is changed into CO behind partial regeneration
2Gas line speed is 3.0～7.6m/s in the dilute phase transfer lime, 690.6～773.9 ℃ of temperature.Catalyzer and regenerated flue gas by the outlet of dilute phase pipe slightly revolve or the sharp separation facility separates, one section is share a dilute phase section catalyst sedimentation is separated with two sections, and through secondary cyclone to energy-recuperation system.Catalyzer continues to burn residual charcoal at second section.These patent characteristics: one section is fast bed, burns the higher 500～700kg/ht of intensity, but about two sections very low 0.2m/s of gas line speed, the very big 500～700kg/m of density of catalyst
3, two sections charcoals that only burn about 10%, reserve is bigger again, and does not obtain reasonable use.Therefore it is also little on average always to burn intensity.
U.S. Patent number USP4,332,674th, adopt two independently turbulent bed two-stage regenerations, one section is incomplete regen-eration, gas line speed is 0.6～0.75m/s, 630～700 ℃ of regeneration temperatures, oxygen level 0～0.5% in the regenerated flue gas.Section continuation regeneration of catalyzer to two behind one section partial regeneration, two sections is heat regeneration, regeneration temperature is 690～800 ℃, gas line speed 0.4～0.7m/s, oxygen level is 3～6% in the regenerated flue gas.Two sections supply respectively to contain the oxygen regeneration gas, and the two-stage regeneration flue gas is a shunting.These patent characteristics: two revivifiers have block form and two kinds of patterns of coaxial-type, and second section revivifier adopts efficient single-stage outward turning, are arranged on outside the device, and deacration distribution rings in the device, no internals can be high temperature resistant 900 ℃.Because the two-stage regeneration device is the low-speed turbulent bed, resistance to mass transfer is big, and one section burns intensity is 100～150kg/ht, and two sections burn intensity is 60～100kg/ht, and two-stage regeneration device inner catalyst reserve is big.The working pressure of two-stage regeneration device is inequality, and regenerated flue gas is again a shunting, needs recovered energy respectively, so energy-recuperation system is complicated, and recovered energy is few, device energy expenditure height.
In existing catalyzer two-stage regeneration, one section or two sections burn for the low-speed turbulent bed, and the burning process of catalyst regeneration, mainly be subjected to the control of oxygen mass transfer speed, therefore, because gas line speed is lower, resistance to mass transfer is big, gas, affixed to touch efficient low, makes two-stage regeneration not bring into play due usefulness.
The objective of the invention is the two-stage regeneration of existing fluidized catalytic cracking catalyst is improved, proposed raising turbulent bed linear speed and with the placed in-line two-stage regeneration of coke-burning riser.
Technical characterstic of the present invention is: first section regeneration, reclaimable catalyst in coke-burning riser, at linear gas velocity 2～8m/s, 630～710 ℃ of temperature, the regenerated flue gas oxygen level is greater than under the 4V% condition, catalyzer is burnt (is the partial regeneration catalyzer to call this catalyzer in the following text) behind the part of coke, with regenerated flue gas and stream or with enter turbulent bed after regenerated flue gas separates, at linear gas velocity 1～3m/s, 680～750 ℃ of temperature, the regenerated flue gas oxygen level continues to burn greater than under the 0.5V% condition, obtains regenerated catalyst.A regenerated catalyst enters reactor, and another part returns coke-burning riser, burns temperature with raising.
Be described in detail content of the present invention and characteristics below in conjunction with accompanying drawing.
Fig. 1 is the synoptic diagram of the catalyst regeneration process of coke-burning riser of the present invention and turbulent bed coaxial-type layout.Contain the coke reclaimable catalyst and enter the bottom of coke-burning riser [2], mixes, contain the oxygen resurgent gases, to coke-burning riser [2], burn by sparger [8] through managing [7] with regenerated catalyst from regenerated catalyst outer circulating tube (to call outer circulating tube in the following text) [3] by pipe [1].Partial regeneration catalyzer and regenerated flue gas and the grid distributor of flowing through [4] to the turbulent bed [5] of revivifier [6], contain the oxygen resurgent gases and enter turbulent bed through pipe [9].Proceed to burn at turbulent bed, obtain regenerated catalyst.Part regenerated catalyst enters reactor through pipe [12], carries out the catalytic cracking of hydrocarbon reaction, and another part regenerated catalyst returns coke-burning riser [2] through outer circulating tube [3], to improve the coke-burning riser temperature.Regenerated flue gas enters revivifier dilute phase section [10], behind the catalyzer that cyclonic separator [11] cutting out partial is carried secretly, enters smoke energy recovering system.
Fig. 2 and catalyst regeneration process shown in Figure 1 are identical, and its difference is: Fig. 2 coke-burning riser [2] stretches in the dilute phase section [10] of revivifier [6], and its outlet links to each other with cyclonic separator [13].The partial regeneration catalyzer enters the turbulent bed [5] of revivifier [6] with after flue gas separates.The miscellaneous equipment code name is among Fig. 2: reclaimable catalyst pipe [1], and outer circulating tube [3] contains oxygen regeneration tracheae [7] and [9], sparger [4] and [8], efficient single stage cyclone separator [11], regenerated catalyst is gone into reactor tube [12].
Fig. 3 is that coke-burning riser of the present invention and turbulent bed block form are arranged the catalyst regeneration process synoptic diagram.The reclaimable catalyst that contains coke enters coke-burning riser upper flow section [2] by pipe [1], mixes mutually with regenerated catalyst from outer circulating tube [4].Contain the oxygen resurgent gases and enter coke-burning riser upper flow section [2] through sparger [6] by pipe [5].After catalyzer is burnt part of coke in coke-burning riser upper flow section [2] and dirty section [3], partial regeneration catalyzer and regenerated flue gas also flow to into containing oxygen regeneration tracheae [7], after containing the oxygen resurgent gases and mixing, enter turbulent bed [9] through grid distributor [8], proceed regeneration, burn residual charcoal.Part regenerated catalyst enters reactor through pipe [10], and another part regenerated catalyst returns coke-burning riser upper flow section [2] through outer circulating tube [4].Enter the regenerated flue gas of revivifier [11] dilute phase section [12], tell the part catalyzer of carrying secretly through cyclonic separator [13] after, enter energy-recuperation system.
Fig. 4 and catalyst regeneration process shown in Figure 3 are identical, and its difference is: dirty section outlet of Fig. 4 coke-burning riser [3] extend in the turbulent bed [9], and is positioned at the top of sparger [8].Among Fig. 4: the miscellaneous equipment code name is: reclaimable catalyst pipe [1], contains oxygen regeneration tracheae [5] and [7], distribution pipe [6] and [8] at coke-burning riser upper flow section [2], revivifier [11] dilute phase section [12], outer circulating tube [4], regenerated catalyst are gone into reactor tube [10], cyclonic separator [13].
Fig. 1 extremely operational condition of catalyst regeneration process shown in Figure 4 is coke-burning riser:
It is exhausted that the catalyst regeneration working pressure is generally 0.2～0.4MPa(), the time of burning is generally less than 3min.
Advantage of the present invention is:
1, one section is adopted coke-burning riser, gas line speed height, and gas-solid two-phase is more near piston flow, the oxygen partial pressure height, catalyst regeneration speed is fast.Two sections is the high velocity turbulent flow bed, gas-solid contact efficiency height.Two sections on average always burn the high 250～400kg/ht of intensity, improve 1.5～3 times than existing two-stage regeneration, have reduced the reclaim equiment investment.
2, compare with existing two-stage regeneration, catalyst inventory can reduce to 30～40%, under the condition of identical live catalyst magnitude of recruitment, has improved the rate of displacement of catalyzer, and equilibrium catalyst activity is improved, and the product that helps the hydro carbons catalyzed reaction distributes.
3, coke-burning riser is simple in structure, and the shared dilute phase section of two-stage regeneration flue gas has been simplified energy-recuperation system, saves energy and facility investment.
4, the present invention transforms favourable especially to the single hop regeneration of existing catalytic cracking unit, and reaction-regeneration system only need be set up coke-burning riser, existing two device framework absolute altitudes can satisfy the pressure equilibrium requirement.Two devices change workload is little, reduced investment, short construction period.
Embodiment
An one cover year treatment capacity is the 0.1Mt fluidized catalytic cracker, the coke-burning riser that proposes by the present invention empyreumatic two-stage regeneration of connecting with turbulent bed carries out catalyst regeneration, and coke-burning riser makes charcoal 50%, annealing in hydrogen atmosphere 100%, the main operational condition of its regeneration section and result such as following table:
The conventional two-stage regeneration of the present invention
Regeneration pressure MPa(is exhausted) 0.3 0.3
First section (coke-burning riser) regeneration temperature, ℃ 690 670
Second section (turbulent bed) regeneration temperature, ℃ 730 730
First section (coke-burning riser) gas line speed, m/s 3 1.0
Second section (turbulent bed) gas line speed, m/s 2.0 0.7
First section (coke-burning riser) outlet oxygen content of smoke gas V% 8.0 2.0
Second section (turbulent bed) outlet oxygen content of smoke gas V% 2.0 4.0
First section (coke-burning riser) 50% amount of the making charcoal kg/h 500 500 that makes charcoal
First section (coke-burning riser) annealing in hydrogen atmosphere amount, kg/h 85 70
Second section (turbulent bed) 50% amount of the making charcoal kg/h 500 500 that makes charcoal
Second section (turbulent bed) annealing in hydrogen atmosphere amount, kg/h-15
Total amount of coke of burning, kg/h 1,085 1085
First section (coke-burning riser) catalyst inventory, t 0.76 3.8
Second section (revivifier) catalyst inventory, t 2.84 5.15
Two-stage regeneration catalyzer general reserve, t 3.6 8.95
Total intensity is burnt in regeneration, and kg/t.h 300 121
Burn the time, min 2.5 6.2
First section heat-obtaining of second section heat-obtaining of heat-obtaining
Claims (7)
1, a kind of two-stage regeneration of fluidized catalytic cracking of hydrocarbons catalyzer, comprising:
(1) catalyzer that contains coke is to coke-burning riser, and at gas line speed 2～8m/s, 630～710 ℃ of regeneration temperatures, regenerated flue gas oxygen level are burnt catalyzer top coke greater than under the 4v% condition, obtain the partial regeneration catalyzer,
(2) the partial regeneration catalyzer is to turbulent bed, at gas line speed 1～3m/s, and 680～750 ℃ of regeneration temperatures, the regenerated flue gas oxygen level is proceeded to burn greater than under the 0.5v% condition, obtains regenerated catalyst,
(3) a part of regenerated catalyst enters reactor, and another part regenerated catalyst returns coke-burning riser.
2, according to the described catalyst regeneration process of claim 1, it is characterized in that: contain the coke catalyzer after coke-burning riser is burnt part of coke, the partial regeneration catalyzer enter be positioned at coke-burning riser top and with the turbulent bed of the revivifier of coke-burning riser coaxial arrangement, continue to burn.
3, according to the renovation process of the described catalyzer of claim 2, it is characterized in that: partial regeneration catalyzer and flue gas and stream or with after flue gas separates, enter the revivifier turbulent bed, continue to burn.
4, according to the described catalyst regeneration process of claim 1, it is characterized in that: the catalyzer that contains coke is after coke-burning riser is burnt part of coke, and the partial regeneration catalyzer enters the revivifier turbulent bed that is arranged in juxtaposition with coke-burning riser, continues to burn.
5, according to the renovation process of the described catalyzer of claim 4, it is characterized in that: the partial regeneration catalyzer mixes the back or directly enters the revivifier turbulent bed with the oxygen resurgent gases that contains of people's turbulent bed, continues to burn.
6, according to the described catalyst regeneration process of claim 1, it is characterized in that: contain the oxygen resurgent gases and enter coke-burning riser and turbulent bed respectively or all enter coke-burning riser.
7, according to the described catalyst regeneration process of claim 1, it is characterized in that: can adopt hot holomorphosis or add CO (carbon monoxide converter) combustion promoter holomorphosis or the carbon monoxide partial combustion.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 92103780 CN1065286A (en) | 1992-05-25 | 1992-05-25 | Improved two-stage regeneration for fluid catalytic cracking catalyst |
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| CN 92103780 CN1065286A (en) | 1992-05-25 | 1992-05-25 | Improved two-stage regeneration for fluid catalytic cracking catalyst |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1126602C (en) * | 1997-09-08 | 2003-11-05 | 许恒波 | High efficiency regenerating technology for molecular sieve catalyst |
| CN101327445B (en) * | 2008-06-12 | 2010-06-09 | 中国石油化工股份有限公司 | High-efficient regeneration method for preparing low carbon olefins catalyst from oxygen-containing compounds |
| CN102463138A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Two-stage Regeneration Method of SAPO-34 Catalyst |
| 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 |
| CN105396518A (en) * | 2015-11-10 | 2016-03-16 | 清华大学 | Coal gasification ash oxidation decarburization combined circulating fluidized bed reactor |
| CN105441131A (en) * | 2015-11-10 | 2016-03-30 | 清华大学 | Method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues |
| CN106732823A (en) * | 2016-11-16 | 2017-05-31 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
| CN104549567B (en) * | 2013-10-17 | 2017-07-25 | 中国石油化工股份有限公司 | Reduce the catalyst recovery process of nitride in flue gas |
-
1992
- 1992-05-25 CN CN 92103780 patent/CN1065286A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1126602C (en) * | 1997-09-08 | 2003-11-05 | 许恒波 | High efficiency regenerating technology for molecular sieve catalyst |
| CN101327445B (en) * | 2008-06-12 | 2010-06-09 | 中国石油化工股份有限公司 | High-efficient regeneration method for preparing low carbon olefins catalyst from oxygen-containing compounds |
| CN102463138A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Two-stage Regeneration Method of SAPO-34 Catalyst |
| CN102463138B (en) * | 2010-11-17 | 2013-08-14 | 中国石油化工股份有限公司 | Two-stage regeneration method for SAPO-34 catalysts |
| 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 |
| 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 |
| CN104549567B (en) * | 2013-10-17 | 2017-07-25 | 中国石油化工股份有限公司 | Reduce the catalyst recovery process of nitride in flue gas |
| CN105396518A (en) * | 2015-11-10 | 2016-03-16 | 清华大学 | Coal gasification ash oxidation decarburization combined circulating fluidized bed reactor |
| CN105441131A (en) * | 2015-11-10 | 2016-03-30 | 清华大学 | Method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues |
| CN105441131B (en) * | 2015-11-10 | 2018-04-20 | 清华大学 | A kind of method of coal gasification lime-ash oxidation and decarbonization ash content coproduction steam |
| CN105396518B (en) * | 2015-11-10 | 2018-11-23 | 清华大学 | A kind of combination circulating fluid bed reactor of coal gasification lime-ash oxidation and decarbonization |
| CN106732823A (en) * | 2016-11-16 | 2017-05-31 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
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