CN201313049Y - Catalyst multi-stage regeneration device - Google Patents
Catalyst multi-stage regeneration device Download PDFInfo
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- CN201313049Y CN201313049Y CNU2008202212781U CN200820221278U CN201313049Y CN 201313049 Y CN201313049 Y CN 201313049Y CN U2008202212781 U CNU2008202212781 U CN U2008202212781U CN 200820221278 U CN200820221278 U CN 200820221278U CN 201313049 Y CN201313049 Y CN 201313049Y
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Abstract
The utility model relates to a catalyst multi-stage regeneration device which comprises a gas-solid separation element arranged in a dilute phase space at the upper part of the device and a smoke pipe line arranged at the top of the device, the device is formed by combining a one-stage turbulent fluidized bed regenerator, a two-stage turbulent fluidized bed regenerator and a three-stage turbulent fluidized bed regenerator in a series connection manner, wherein, the three-stage turbulent fluidized bed regenerator is configured with a fresh air gas distributor, a distribution plate or partition board is arranged on each-stage turbulent fluidized bed regenerator, all the regenerators are communicated through distribution plates, catalyst return pipes or delivery pipes, a spent catalyst standpipe and a regenerated catalyst standpipe are respectively arranged at the bottoms of the one-stage turbulent fluidized bed regenerator and the three-stage turbulent fluidized bed regenerator, and all the stages of the turbulent fluidized bed regenerators are coaxially arranged. The catalyst regeneration device adopts the multi-stage upflow regeneration method, so that the average chemical kinetic speed is increased; since all the stages of the turbulent fluidized bed regenerators are coaxially arranged in an overlapped manner, the height of the device is reduced, the oilgas pipe line is shortened and the engineering investment is reduced; the consumption of the oxygen-containing gas can be saved, and the production cost is reduced; and the required catalyst reserve is less, the residence time of the catalyst is shortened, the metal contamination of the catalyst is reduced and the activity is improved.
Description
Technical field
The utility model relates to a kind of petroleum hydrocarbon catalytic conversion technique, particularly relates to a kind of catalyst multistage regenerating unit.
Background technology
The regeneration of coked catalyst is the requisite technical process of hydrocarbon raw material fluidized catalytic conversion process, and occupy very big proportion in the investment of making an investment in whole catalytic convention design of regenerator, its energy consumption also accounts for more than 80% of catalytic convention design energy consumption, and the electric energy that this energy consumption mainly consumes from the compression regeneration gas, improve the medium utilization rate, improve regeneration effect, to reducing the device operating cost, it is significant to reduce construction investment.Therefore catalyst regeneration technology and device thereof are hot issues of catalyzed conversion area research always.
Industrial regeneration commonly used mainly contains at present: single hop regeneration, two-stage regeneration and circulation fluidized bed regeneration etc.The single hop regeneration technology is fairly simple, equipment is also uncomplicated, be widely adopted always, but for giving full play to the activity of such catalysts effect, often require the requirement of regenerated catalyst carbon containing to be lower than 0.1%, regenerate for single hop, realize comparatively difficulty of this requirement, the reserve and the recovery time that increase catalyst need be arranged, need to consume more regenerative response gas, plant energy consumption and operating cost are higher.Its unfavorable factor mainly is that single hop fluidization bed back-mixing is serious, and catalyst regeneration efficient is lower; The two-stage regeneration mode then is to regenerate to carry out in two fluid beds successively, and two sections comprehensive regeneration effect is better than single hop regeneration, and catalyst inventory and recovery time are lower, therefore becomes the comparatively general a kind of reconstituted form of present application.
Technology about two-stage regeneration has a lot, a kind of FCC catalyst recovery process is disclosed in its patent EP0610186 as MOBIL company, comprise following two steps: spent agent at first partly is regenerated as half regenerated catalyst in the one section regenerator that comprises a fast fluidized bed and dilute phase conveying standpipe, one section regenerated flue gas does not enter two sections regeneration, but after isolating catalyst, discharge regenerator, half regenerated catalyst enters two sections fluid beds and contacts with the fresh regenerated air again, further regeneration, generate regenerative agent and flue gas, oxygen content is all higher in one section and the two sections regenerated flue gas, so oxygen consumption index and energy consumption index are all higher; The patent US3844973 of Uop Inc. discloses a kind of fluidized catalyst renovation process, first section is fast fluidized bed (burning jar) and dilute phase carrier pipe, after gas solid separation, regenerated catalyst enters second dense bed Returning reactor after stripping goes out flue gas and uses, regenerated flue gas then after the cyclone separator on top is further isolated catalyst, is discharged through the flue gas pipeline; Another patent US4849091 of Uop Inc. then discloses a kind of catalyst segments renovation process, be with the US3844973 difference: catalyst enters dense bed renewing zone (i.e. second dense bed) at last and contacts realization holomorphosis again with new air, regenerated catalyst part Returning reactor uses, and a part is returned efficient contact zone (i.e. first dense bed); Chinese patent CN200410030876.7 then discloses the combined type catalyzed conversion renovation process of a kind of pair of regenerator, it is made up of two regenerating units arranged side by side, comprise turbulent bed first regenerator and postposition second regenerating unit that contains regenerating tube, spent agent at first enters turbulent bed regenerator partial regeneration, half regenerated catalyst and containing water vapor flue gas rise to the regenerator dilute phase, flue gas is directly discharged regenerator again and again after gas solid separation, half regenerated catalyst enters rearmounted regenerating tube and continue regeneration under the new air conditions that replenishes, since again and again with two again in the flue gas oxygen content all higher, so oxygen consumption index and energy consumption index are all higher.More than these intensifying regenerating technology the high 1-2 of the conventional single hop regenerator of regenerator regeneration strength ratio doubly, but its structure and operate all more complicated, and do not consider the problem of utilizing of excess oxygen in the flue gas, excess oxygen is discharged from pipeline in the flue gas, causes actual consumption to increase.
LPEC discloses a kind of two-stage oxidizing regenerative method of fluid catalyst in its CN89109293.5, two-stage regeneration gas adopts serial flow up and down, first section regeneration is located at the bottom, second section regeneration is located at top, reclaimable catalyst is behind first section regenerative response, catalyst and regenerated flue gas upwards flow into second section regeneration together, have simplified reclaim equiment structure and technological process; But two-stage oxidizing is and flows regeneration, the reaction that contacts with low oxygen content regenerated flue gas after first section regeneration of the catalyst of second section low carbon content, and chemical kinetics speed is low, is difficult to realize the overall raising of regeneration efficiency.
Uop Inc. and Ashland company disclose the RCC two-phase up-flow regeneration reaction regeneration equipment of its joint development in US4299687, by first regenerator of arranged superposed up and down and second regenerator and one and its reacting-settler that just is arranged in juxtaposition formed; Two regenerators are arranged up and down, first regenerator is arranged on top, second regenerator is arranged on the bottom, come the reclaimable catalyst of autoreactor to be introduced into first regenerator of top, half regenerative agent continues regeneration by the catalyst standpipe by second regenerator that gravity flows into the below, fresh regenerated gas is introduced into second regenerator of below, and the oxygen gas of second regenerator enters first regenerator to be continued to utilize.Though it has improved regeneration effect, can satisfy the requirement on technology and the engineering, and utilize the O that contains of second regenerator top discharge
2Flue gas, but because reclaimable catalyst enters first regenerator through inclined tube, the determining positions that first regenerator is higher relatively device highly obviously strengthen, the high 20m of generally more conventional catalytic convention design (total height is generally more than 70m), cause build and recondition expense all higher.
CN97121795.5 discloses a kind of heavy oil fluidized catalyzed conversion eclipsed form two-stage regeneration technology, disclosed RCC technology is similar among its technological process aspect and the above-mentioned US4299687, only different on equipment inner structure, logical repeatedly between the two-stage regeneration device with the low pressure drop distribution grid, have equally that the RCC process unit is too high to cause investing bigger problem.
CN01114931.0 has also proposed a kind of fluidized catalytic conversion catalyst recovery process, the catalyst tandem compound regeneration that the tubular type regenerator is mutually arranged side by side with multistage turbulent bed regenerator, catalyst enters from regenerator bottoms, be transported to the regenerator section on top through carrier pipe, burn the carbon of 40-50% and almost whole hydrogen at carrier pipe simultaneously, flue gas and catalyst are transported to regenerator top together, regenerate through multistage counter current in the turbulent bed regenerator then, finish whole regenerative processes.This method is because the turbulent bed regenerator is taked the multistage counter current regeneration, and average chemical kinetics velocity ratio is higher, has improved the regeneration effect of catalyst, but owing at first adopt tubular type regeneration, the initial reaction temperature of spent agent is lower, is difficult to meet the demands.
Summary of the invention
Technical problem to be solved in the utility model is on the basis of existing catalyst regeneration device, develop a kind of can the intensifying regenerating process, can reduce the catalyst multistage regenerating unit of construction investment and operation energy consumption again.
The technical solution adopted in the utility model is as follows:
Catalyst regeneration multistage device of the present utility model, be included in device top dilute phase space the gas solid separation element, be located at the flue gas pipeline at device top, regenerating unit is formed by one section, two sections, three sections turbulent bed regenerator tandem compounds, three sections regenerator configuration fresh air gas distributors, each section regenerator is provided with distribution grid or dividing plate, adopt distribution grid or catalyst return duct or carrier pipe to be communicated with between regenerator, one section and three sections regenerator bottoms are provided with reclaimable catalyst standpipe and regenerated catalyst standpipe respectively, each section regenerator coaxial arrangement.
Catalyst multistage regenerating unit of the present utility model, one of optimized technical scheme is: one section regeneration is located at the middle part, and two sections regeneration are located at top, and three sections regeneration are located at the bottom; Between one section and two sections, one section and three sections regenerators distribution grid is set, two sections are communicated with by the catalyst return duct with three sections regenerators, on the catalyst return duct guiding valve are set, and catalyst backflow quantity is controlled by guiding valve.
The further improved technical measures of scheme one can be: be one section and two sections regenerator configuration fresh air gas distributors, so that replenish fresh compressed air to one section and two sections regenerative responses, promptly on three sections tops three sections with an intersegmental distribution grid below with one section on one section top and two intersegmental distribution grids below gas distributor is set.The gas distributor of abovementioned technology also can be arranged on the distribution grid top.
The further improved technical measures of scheme one also can be: be one section or two sections regenerator configuration fresh air gas distributors, so that to one section or two sections additional fresh compressed air of regenerative responses, promptly on three sections tops three sections with an intersegmental distribution grid below be one section regenerator configuration fresh air gas distributor, or on one section top one section with two intersegmental distribution grids below be that two sections regenerators dispose the fresh air gas distributors.The gas distributor of abovementioned technology also can be arranged on the distribution grid top.
Catalyst multistage regenerating unit of the present utility model, two of optimized technical scheme is: one section regeneration is located at the bottom, two sections regeneration are located at top, three sections regeneration are located at the middle part, one section regenerator configuration fresh air gas distributor, between one section and three sections regenerators dividing plate is set, between two sections and three sections regenerators distribution grid is set, three intersegmental parts are provided with one section regenerated flue gas and catalyst and two intersegmental carrier pipes, two sections are communicated with by the catalyst return duct with three sections regenerators, and two sections are communicated with by the catalyst return duct with one section regenerator.The design of distribution grid does not allow catalyst to land downwards, this optimized technical scheme, one section regenerated flue gas and catalyst enter two sections through carrier pipe and distribution grid and continue regeneration, half regenerated catalyst portion in two sections refluxes through the catalyst return duct between two sections and one section regenerator and enters one section regenerator improving the initial reaction temperature of spent agent in one section regenerative response, and part enters three sections regenerators to finish whole regeneration through the catalyst return duct between two sections and three sections regenerators.
The further improved technical measures of scheme two can be on three sections tops below three sections and the two intersegmental distribution grids, one section top with two intersegmental carrier pipes is provided with the flue gas path, make regenerated flue gas in three sections on three sections tops below three sections and the two intersegmental distribution grids with from one section regenerated flue gas and catalyst mix, enter two sections regenerators through distribution grid together.
The further improved technical measures of scheme two can also be that the catalyst return duct between two sections and three sections regenerators is arranged on regenerator when outer, on the catalyst return duct guiding valve are set.
Catalyst multistage regenerating unit of the present utility model, three of optimized technical scheme is: one section regenerator is located at the bottom, two sections regenerators are located at the middle part, three sections regenerators are located at top, one section is all disposed the fresh air gas distributor with two sections regenerators, between one section and two sections regenerators dividing plate is set, and between two sections and three sections regenerators distribution grid is set, two intersegmental parts are provided with one section regenerated flue gas and catalyst and two intersegmental carrier pipes, and three sections are communicated with by the catalyst return duct with one section regenerator.
The further improved technical measures of scheme three are two sections and are communicated with by the catalyst return duct with three sections regenerators that this return duct can be arranged in the regenerator, also can be arranged on outside the regenerator.
The further improved technical measures of scheme three can also be two sections and be communicated with by the catalyst return duct with three sections regenerators that this return duct is arranged on outside the regenerator, on the catalyst return duct guiding valve is set.
In all schemes of catalyst multistage regenerating unit of the present utility model, when each section regenerator disposed distribution grid and gas distributor simultaneously, the gas distributor of this section or be arranged on distribution grid below perhaps was arranged on the distribution grid top.
The catalyst multistage regenerating unit that the utility model proposes has the following advantages:
1, the utility model adopts multistage counter current regeneration, make high keto content gas and the phase reaction of low carbon content catalyst, and low oxygen content gas contacts with the high-carbon content catalyst, has improved average chemical kinetics speed, has strengthened regenerative process;
2, the folded formula coaxial arrangement of each section regenerator has realized that reclaimable catalyst from regenerator bottoms or middle part charging, has reduced corresponding catalytic convention design height, has shortened oil-gas pipeline, reduces construction investment;
3, because the utility model is multistage regeneration, can adopt distribution grid to connect between each section, help making full use of the flue gas that each section contains a certain amount of excess oxygen, thereby can save the oxygen-containing gas consumption, reduce producing cost;
4, owing to finally only discharge one flue gas, overcome some cross-flow two-stage regeneration device and produced two strands of flue gases need to handle or prevent respectively the tail combustion when mixing problem.
5, the catalyst inventory of Xu Yaoing is few, reduces the time of staying of catalyst, reduces the metallic pollution of catalyst, improves active.
Description of drawings
Fig. 1: one section regeneration of the utility model is located at the middle part, and two sections regeneration are located at top, and three sections regeneration are located at the regenerating unit structural representation of bottom.
Fig. 2: one section regeneration of the utility model is located at the bottom, and two sections regeneration are located at top, and three sections regeneration are located at the regenerating unit structural representation at middle part.
Fig. 3: the another kind of one section regeneration of the utility model is located at the bottom, and two sections regeneration are located at top, and three sections regeneration are located at the regenerating unit structural representation at middle part.
Fig. 4: one section regeneration of the utility model is located at the bottom, and two sections regeneration are located at the middle part, and three sections regeneration are located at the regenerating unit structural representation on top.
Fig. 5: the another kind of one section regeneration of the utility model is located at the bottom, and two sections regeneration are located at the middle part, and three sections regeneration are located at the regenerating unit structural representation of bottom.
Fig. 6: the utility model embodiment device structural representation.
The specific embodiment
Describe the technical solution of the utility model in detail below in conjunction with accompanying drawing, but protection domain of the present utility model includes, but are not limited to this:
As shown in Figure 1: one section regenerator I is located at the middle part, and two sections regenerator II are located at top, and three sections regenerator III are located at the bottom; I is communicated with by distribution grid 15,18 respectively with III with II, I, and II is communicated with by catalyst return duct 19 with III; I, II and III dispose gas distributor 14,17,22 respectively.
As shown in Figure 2: one section regenerator I is located at the bottom, and two sections regenerator II are located at top, and three sections regenerator III are located at the middle part; I is communicated with II by carrier pipe 31 and distribution grid 32, and II is communicated with by distribution grid 32 with III; Dividing plate 30 is set between I and the III, and II and I, II and III are provided with catalyst return duct 33,35 respectively; I and III dispose gas distributor 29,38 respectively.34,36 is guiding valve.
As shown in Figure 3: the catalyst return duct 39 between II and III is arranged in the III, does not establish guiding valve, in carrier pipe 31 side wall upper part flue gas path 40 is set.Regenerated flue gas among the III mixes with catalyst and flue gas logistics in the carrier pipe 31 by flue gas path 40, enters among the II together.Other same Fig. 2.
As shown in Figure 4: one section regenerator I is located at the bottom, and two sections regenerator II are located at the middle part, and three sections regenerator III are located at top; I is communicated with by carrying standpipe 41 with II, and II is communicated with by distribution grid 46 with III; Dividing plate 30 is set between I and the II, catalyst return duct 47,49 is set respectively between III and I, III and II; I, II and III dispose gas distributor 29,43,45 respectively.48,50 is guiding valve.
As shown in Figure 5: do not establish the catalyst return duct between III and the II; Gas distributor 45 is located at distribution grid 46 tops.Other same Fig. 4.
Of the present utility model concrete regenerative process shown in Figure 6 is: from the fresh oxygen-containing gas 13 that is used for one section regeneration of gas distributor 14, with merge from whole flue gases of bottom III and part catalyst after enter I through distribution grid 15, mix with the reclaimable catalyst 10 that enters the I bottom through guiding valve 11 to be generated, reclaimable catalyst standpipe 12, carry out one section regeneration; Catalyst is reacted flue gas and the unreacted oxygen-containing gas of part is delivered to I top, mixes with the fresh oxygen-containing gas 16 that replenishes that is used for two sections regeneration, enters the two sections regenerator II in top through distribution grid 18 and carries out two sections regeneration; Regeneration back regenerated flue gas 27 enters superjacent air space, discharge by flue gas pipeline 26 isolate the catalyst of carrying secretly through cyclone separator 25 after, catalyst is back to III through return duct 19, guiding valve 20, mix with the fresh oxygen-containing gas 21 that is used for three sections regeneration and to finish whole regenerative processes, regenerated catalyst 23 is by regenerated catalyst standpipe 24 Returning reacting systems.
Embodiment:
Embodiment: certain is 100 * 10 years old
4The t/a catalytic cracking unit is regenerated with 200 ℃ compressed air.As Fig. 6 and shown in Figure 1, spent agent 10 carbon contents are 1.3%, 490 ℃ of temperature, and regenerative agent 23 carbon contents of outflow are 0.05%, oxygen content about 1% in the regenerator outlet flue gas 27. Distribution grid 15,18 via hole flow velocitys are 15-20m/s, and the catalytic amount that returns through return duct 19 is 2.5 times of spent agent internal circulating load, and wherein 1.5 times enter one section regenerator by distribution grid 15, improve one section regeneration temperature.Two sections interior catalyst of regenerator enter three sections after external warmer 50 coolings, 51 is guiding valve.
Each section regeneration temperature, intake, gas void tower flow velocity, burn ratio and the device altitude information as follows:
I section II section III section
Regeneration temperature/℃ 685 700 680
Intake/% 80 0 20
Gas void tower flow velocity/m/s 1.5 0.7 1.0
The ratio of burning/% 70-80 15-25 5-10
Device height/m 84 (the close phase of catalyst) 6
Claims (10)
1, a kind of catalyst multistage regenerating unit, comprise the gas solid separation element of being located at device top dilute phase space, the flue gas pipeline of being located at the device top, it is characterized in that: regenerating unit is formed by one section, two sections, three sections turbulent bed regenerator tandem compounds, three sections regenerator configuration fresh air gas distributors, each section regenerator is provided with distribution grid or dividing plate, adopt distribution grid or catalyst return duct or carrier pipe to be communicated with between regenerator, one section and three sections regenerator bottoms are provided with reclaimable catalyst standpipe and regenerated catalyst standpipe respectively, each section regenerator coaxial arrangement.
2, according to the described catalyst multistage regenerating unit of claim 1, it is characterized in that: one section regeneration is located at the middle part, and two sections regeneration are located at top, and three sections regeneration are located at the bottom; Between one section and two sections, one section and three sections regenerators distribution grid is set, two sections are communicated with by the catalyst return duct with three sections regenerators, on the catalyst return duct guiding valve are set, and catalyst backflow quantity is controlled by guiding valve.
3, according to the described catalyst multistage regenerating unit of claim 2, it is characterized in that: be one section and two sections regenerator configuration fresh air gas distributors.
4, according to the described catalyst multistage regenerating unit of claim 2, it is characterized in that: be one section or two sections regenerator configuration fresh air gas distributors.
5, according to the described catalyst multistage regenerating unit of claim 1, it is characterized in that: one section regeneration is located at the bottom, two sections regeneration are located at top, three sections regeneration are located at the middle part, one section regenerator configuration fresh air gas distributor, between one section and three sections regenerators dividing plate is set, between two sections and three sections regenerators distribution grid is set, three intersegmental parts are provided with one section regenerated flue gas and catalyst and two intersegmental carrier pipes, two sections are communicated with by the catalyst return duct with three sections regenerators, and two sections are communicated with by the catalyst return duct with one section regenerator.
6, according to the described catalyst multistage regenerating unit of claim 5, it is characterized in that: on three sections tops below three sections and the two intersegmental distribution grids, one section top with two intersegmental carrier pipes is provided with the flue gas path.
7, according to the described catalyst regeneration device of claim 1, it is characterized in that: one section regenerator is located at the bottom, two sections regenerators are located at the middle part, three sections regenerators are located at top, one section is all disposed the fresh air gas distributor with two sections regenerators, between one section and two sections regenerators dividing plate is set, and between two sections and three sections regenerators distribution grid is set, two intersegmental parts are provided with one section regenerated flue gas and catalyst and two intersegmental carrier pipes, and three sections are communicated with by the catalyst return duct with one section regenerator.
8, according to the described catalyst multistage regenerating unit of claim 7, it is characterized in that: two sections are communicated with by the catalyst return duct with three sections regenerators.
9, according to claim 5,6 or 8 described catalyst multistage regenerating units, it is characterized in that: the catalyst return duct between two sections and three sections regenerators is arranged on regenerator when outer, on the catalyst return duct guiding valve is set.
10, according to the described catalyst multistage regenerating unit of claim 1, it is characterized in that: when each section regenerator disposed distribution grid and gas distributor simultaneously, the gas distributor of this section or be arranged on distribution grid below perhaps was arranged on the distribution grid top.
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2008202212781U CN201313049Y (en) | 2008-11-19 | 2008-11-19 | Catalyst multi-stage regeneration device |
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2008202212781U CN201313049Y (en) | 2008-11-19 | 2008-11-19 | Catalyst multi-stage regeneration device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104419457A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device employing double lift pipes |
| CN104419458A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN106753510A (en) * | 2017-01-25 | 2017-05-31 | 中国石油天然气股份有限公司大连石化分公司 | A kind of regenerator in catalytic cracking unit |
-
2008
- 2008-11-19 CN CNU2008202212781U patent/CN201313049Y/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104419457A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device employing double lift pipes |
| CN104419458A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN104419457B (en) * | 2013-09-09 | 2016-05-11 | 中石化洛阳工程有限公司 | A kind of double lift pipe catalytic cracking method and device |
| CN104419458B (en) * | 2013-09-09 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of catalyst cracking method and device |
| CN106753510A (en) * | 2017-01-25 | 2017-05-31 | 中国石油天然气股份有限公司大连石化分公司 | A kind of regenerator in catalytic cracking unit |
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Granted publication date: 20090923 Termination date: 20121119 |