CN103387477B - System and process for preparing olefin from organic oxygen-containing compound for reducing catalyst coking - Google Patents
System and process for preparing olefin from organic oxygen-containing compound for reducing catalyst coking Download PDFInfo
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Abstract
The invention discloses a system and a process for preparing olefin from an organic oxygen-containing compound, which are used for reducing catalyst coking. The system comprises: at least one reactor; at least one regenerator; at least one deactivated catalyst transfer conduit; at least one regenerated catalyst conveying pipeline, wherein the part of the regenerated catalyst conveying pipeline close to the regenerator comprises at least two branch pipes, the part close to the reactor comprises at least one conduit, and the branch pipes and the conduit are communicated with each other; wherein at least one indirect heat exchanger is provided in said at least one branch pipe for cooling the regenerated catalyst entering the branch pipe, the cooled regenerated catalyst being mixed with regenerated catalyst from the other branch pipe at the junction area of said branch pipe and the conduit and entering the reactor through said conduit, thus preventing the regenerated catalyst entering the reactor from being excessively hot and preventing the surface of the regenerated catalyst from being rapidly carbonized when it contacts with the organic oxygen-containing compound in the reactor.
Description
Technical field
The present invention relates to system and the technique thereof of a kind of organic oxygen-containing compound, for example methyl alcohol and/or dme alkene processed, particularly, relate to a kind of system and technique thereof of the organic oxygen-containing compound alkene processed that reduces catalyzer coking.
Background technology
Organic oxygen-containing compound, for example methyl alcohol and/or dme alkene technology processed has been opened up the new technology route by coal production basic organic chemical industry raw material, and wherein typical technology is methanol-to-olefins (MTO).Typically, MTO complete set technology is made up of reaction technology and isolation technique.Reaction technology is designed to core with catalyst preparation and reactor development, taking methyl alcohol as olefin production mixture; Product distributes and purity requirement is the basis of exploitation separating technology.
First MTO reaction is to generate dme by methanol dehydration, and then the equilibrium mixture of dme and methyl alcohol continues to react, and is converted into the low-carbon (LC) mixed olefins as leading taking ethene and propylene.A small amount of low-carbon alkene further generates saturated alkane, aromatic hydrocarbons and high olefin by reactions such as polycondensation, cyclisation, dehydrogenation, alkylation, hydrogen transferences, also has a small amount of carbon deposit reaction.
The whole process of MTO technique can be divided into reaction-regeneration system and reaction gas separation system two portions.Reactive moieties only has gas-solid two-phase, and this catalyzed reaction is thermopositive reaction.The catalyzer of inactivation need be in fluid bed regenerator coke burning regeneration, then, return to fluidized-bed reactor and continue reaction.Reactor and revivifier are all provided with heat-transfering device.
The technique that it is low-carbon alkene through methanol conversion that MTO is actually by synthetic gas.Some famous oil and chemical companies in the world, as Exxon Mobil Corporation (Exxon – Mobil), BASF AG (BASF), AP Oil company (UOP) and Hydro company (Norsk Hydro) all drop into substantial contribution and personnel, years of researches are carried out.
It is reported, the MTO process products composition of UOP/Hydro is comparatively simple, and dopant species and content are less, more easily realize product separation and reclaim, and can in relative broad range, adjust C in reaction product
2product and C
3the ratio of product and the total conversion rate of alkene.The SAPO-34 catalyzer of UOP/Hydro company research and development has suitable inner duct scantlings of the structure and solid acid intensity, can reduce low-carbon alkene oligomerisation, improves the selectivity that generates alkene.Afterwards, UOP/Hydro company has developed new catalyst MTO – 100 again on SAPO – 34 catalyzer bases.
As everyone knows, in the reactive system of organic oxygen-containing compound alkene processed, for example methanol-to-olefins (MTO), the reaction of burning in conversion reaction in reactor and revivifier is thermopositive reaction, and a large amount of heats is taken system out of by the interchanger being arranged in reactor and revivifier.Decaying catalyst in revivifier the temperature after coke burning regeneration up to 600-700 DEG C; although being installed in revivifier, interchanger reduces the temperature in revivifier; with guard catalyst with make Plant in good condition; but the temperature of regenerated catalyst in the standpipe of revivifier bottom is still very high, reaches 630-650 DEG C.Organic oxygen-containing compound, for example methyl alcohol are heated to 160-170 DEG C entering before reactor, comparatively speaking, cold methanol gas is running into suddenly after very hot catalyzer, will be at catalyst surface fast charring, small duct and the active sites of the coke meeting blocking catalyst generating, thereby, the activity of catalyzer and selectivity of light olefin are adversely affected.
In addition, in reactor, methanol conversion is that the ideal response temperature of alkene is 450-480 DEG C, temperature is to participate in the conversion reaction that thermal discharge is 37-53kJ/mol after the high temperature catalyst of 630-650 DEG C enters reactor, after methyl alcohol contacts with catalyzer on the one hand, catalyst surface can be because of high temperature carbonization coking rapidly, causes catalyst deactivation quickening, the quickening of catalyst regeneration frequency, catalyzer to reduce work-ing life; On the other hand, so a large amount of hot polymerization collection has also increased the working load of interchanger in reactor.
For this reason, some investigators have set about research and how suitably to have reduced the temperature that enters the regenerated catalyst in reactor, also ensure whereby the technical problem of catalyst activity to reduce the too fast coking of catalyst surface.For example, CN1918278A disclose a kind of in the operating process of MTO device the method for stabilizing catalyst activity, wherein, after the regeneration of SAPO granules of catalyst, make this regenerated granule with have in its surface coke particle so that the mode that their catalytic activity remains on predeterminated level mix, thereby ensure the activity of catalyzer during conversion reaction.
Aforesaid method has following feature: (1) is in the revivifier that contains the oxygen excessive by stoichiometry, silicoaluminophosphamolecular molecular sieve (SAPO) granules of catalyst is regenerated, make weight taking the molecular screen material in this regenerated catalyst particles as benchmark, coke content is less than about 1wt%; (2) at the temperature that is less than 550 DEG C, by this regenerated catalyst particles with contain at least coking catalyst particle of 2wt% coke and mix; (3) regenerated catalyst particles is mixed with coking catalyst particle at the temperature of about 400-550 DEG C; (4) regenerated catalyst particles was cooled before mixing with coking catalyst particle.
In aforesaid method; although regenerated catalyst is cooled and realize mechanically mixing in coking catalyst particle; but coking catalyst particle is not regeneration; and coke on this part granules of catalyst is difficult to transfer to above the little regenerated catalyst particles of coke content by simple mechanically mixing; therefore; the average coke level of granules of catalyst mixture does not represent the actual coke content of each several part granules of catalyst; therefore, this method is to reducing catalyst surface coking and ensureing that whereby the effect of catalyst activity is limited.
CN1007784B discloses a kind of fluidized particles regeneration and the cooling method and apparatus simultaneously carrying out.It is actually a kind of hot particle of solid combustible (as the catalyzer in FCC refining of petroleum) regeneration (burning) and cooling method and apparatus that is fluidized, wherein, the hot particle of at least a portion flows to cooling room from the first dense phase fluidized bed, carries out heat exchange and cooling in vertical shell-and-tube interchanger with circulating cooling medium.Cooling degree is controlled by the pipe in interchanger and hot intergranular heat transfer coefficient.This coefficient changes with the fluidization gas of sending in interchanger fluidized-bed layer.The bottom of interchanger in cooling room, imports and exports conduit lower than hot particle completely.Therefore, maintenance can be shifted out interchanger when cooling room, and the pipe of interchanger is embedded in the cold granules of catalyst of fluidisation not, thereby reaches the object of protection heat exchanger tube.The fluidized gas that comes from interchanger is introduced in combustion zone, bottom as auxiliary source of the gas, to ensure sufficient combustion.
In aforesaid method and device, described interchanger is back-mixing interchanger, be that cooling hot particle, for example granules of catalyst got back in combustion chamber again as moving thermal medium, for the temperature of control combustion chamber, and then control and do not enter in interchanger and the temperature of the hot particle of part of directly being discharged by hot particle separation district.Therefore, say exactly, what interchanger was cooling is heat transferring medium or heat-transfer medium, and only this heat transferring medium or heat-transfer medium are the hot particles of regenerating through burning.
Therefore, for the granules of catalyst of organic oxygen-containing compound alkene processed, in the time entering in reactor, excess Temperature causes the problem of the rapid coking of catalyst surface, in the urgent need to having a kind of practicality and easy terms of settlement.
The present invention is intended to solve the insoluble technical problem of this prior art, and proposes a kind of system and technique thereof of the organic oxygen-containing compound alkene processed that reduces catalyzer coking.
Summary of the invention
According to a first aspect of the invention, provide a kind of system of the organic oxygen-containing compound alkene processed that reduces catalyzer coking, comprising:
At least one reactor, organic oxygen-containing compound is converted into alkene therein;
At least one revivifier, decaying catalyst is reproduced by burning therein;
At least one decaying catalyst transport pipe, decaying catalyst is entered in described revivifier by described reactor through described pipeline;
At least one regenerated catalyst road, regenerated catalyst is entered in described reactor by described revivifier through described pipeline, described regenerated catalyst road comprises at least two arms near the part of described revivifier, part near described reactor comprises at least one conduit, and described arm and described conduit are interconnected;
Wherein, in above-mentioned at least one arm, there is at least one indirect heat exchanger, for the cooling regenerated catalyst that enters this arm, cooled regenerated catalyst mixes with the regenerated catalyst from other arm at the connecting zone place of described arm and described conduit, and enter in above-mentioned reactor through described conduit, so prevent from entering regenerated catalyst temperature in described reactor too high when preventing that regenerated catalyst from contacting in described reactor with organic oxygen-containing compound surface by fast charring.
Preferably, described organic oxygen-containing compound is methyl alcohol and/or dme; Described alkene is low-carbon alkene; Described catalyzer is SAPO-34, SAPO-18 and/or SAPO-100 catalyzer; Described revivifier is vertical type combustion chamber; Described indirect heat exchanger is recuperative heat exchanger; Described arm is vertical; Described indirect heat exchanger is that vertical, level or inclination are arranged.
In said system, preferably, described system also comprises: regenerated catalyst flowrate control valve, fluidizing agent medium entry pipe, fluidizing agent rate-of flow and/or pressure controlled valve and/or temperature monitoring and control device, wherein, described temperature monitoring and control device are for monitoring and control described reactor, revivifier, arm and conduit, indirect heat exchanger and the regenerated catalyst temperature at different positions place, more preferably, described temperature monitoring and control device regulate temperature automatically according to the result of monitoring, make it within rational scope.
More preferably, in said system, by regulating the opening degree of regenerated catalyst flowrate control valve and the load of indirect type interchanger to regulate the regenerated catalyst temperature entering in above-mentioned reactor reaction bed, be 450-480 DEG C thereby make the temperature of described reactor reaction bed.Concrete way is: the 10-60% that is accounted for regenerated catalyst total amount described at least one in arm by the cooling regenerated catalyst of indirect heat exchanger described at least one; The temperature that enters the regenerated catalyst in above-mentioned reactor is 500-625 DEG C.
According to a second aspect of the invention, provide a kind of technique of said system by organic oxygen-containing compound alkene processed of using, comprising:
(1) in described reactor, pass into organic oxygen-containing compound, organic oxygen-containing compound, under the effect of catalyzer, is converted into the reaction product that comprises alkene;
(2) above-mentioned reaction product is discharged to reactor, and carry out subsequently product separation, thereby obtain alkene;
(3) decaying catalyst is moved in described revivifier by described reactor by described decaying catalyst transport pipe, decaying catalyst is reproduced by burning in described revivifier;
(4) regenerated catalyst is moved in described reactor by described revivifier by described regenerated catalyst road, continues to participate in reaction,
Wherein, regenerated catalyst is being moved in the process in described reactor by described revivifier, part regenerated catalyst is cooling by indirect heat exchanger described at least one in arm described at least one, cooled regenerated catalyst mixes with the regenerated catalyst from other arm at the connecting zone place of described arm and described conduit, and enter in above-mentioned reactor through described conduit, so prevent from entering regenerated catalyst temperature in described reactor too high when preventing that regenerated catalyst from contacting in described reactor with organic oxygen-containing compound surface by fast charring.
Preferably, in above-mentioned technique, described indirect heat exchanger is cooling-water flowing through straight pipe type or coiled pipe cooler therebetween, and this water cooler produces high-temperature steam through heat exchange, and these high-temperature steams can be used as the stripping gas of catalyzer in technological process.
Brief description of the drawings
The Figure of description that forms a specification sheets part of the present invention is used for the present invention to be further explained; accompanying drawing of the present invention and explanation thereof are for explaining in detail the present invention; so that those of ordinary skill in the art are expressly understood essence of the present invention more, it does not form any restriction to protection domain of the present invention.
Fig. 1 is the system of organic oxygen-containing compound of the present invention alkene processed and the schematic diagram of technique thereof.
Embodiment
Be further explained in detail the present invention by the description below with reference to accompanying drawing, but below describe only for making general technical staff of the technical field of the invention can more be expressly understood principle of the present invention and marrow, and do not mean that the present invention is carried out to any type of restriction.
Typically, conversion reaction, for example MTO reaction of organic oxygen-containing compound alkene processed show as one-level rapid reaction on fresh ASPO-34 catalyst surface, catalyzer has best organic oxygen-containing compound in the time that coke content is 2.0-5.0 % by weight, as methanol conversion and olefine selective, the thorough inactivation of catalyzer when coke content reaches 7.5 % by weight.
Therefore, common way is: in revivifier, by burning, catalyst regeneration is participated in to reaction to approximately catalyzer being turned back to when 1.5 % by weight containing charcoal, carried out coke burning regeneration in catalyzer being entered to revivifier from reactor after coke content is greater than 5.0 % by weight in reactor.Reduce as far as possible and when high-temperature regenerated catalyst turns back in reactor, run into the carbon deposit that cold methanol gas moment causes, increase between the active zone of catalyzer, thereby, methanol conversion and olefine selective improved.
According to such theory, as shown in Figure 1, in system of the present invention and technique, one root regeneration standpipe of revivifier (regenerative combustion chamber) bottom is become at least two vertical arms of independently regenerating, the vertical arm of at least two root regenerations merges at least one delivery conduit entering before reactor, enters in reactor, participate in organic oxygen-containing compound conversion of olefines reaction processed from the regenerated catalyst of different arms near meet after mixing.
Specifically, as shown in Figure 1, the high temperature catalyst after regeneration flows at least two vertical arms for delivery of regenerated catalyst simultaneously.Conventionally, be provided with catalyst stream control valve in above-mentioned vertical arm regenerated catalyst ingress and regulate the catalyst amounts entering in above-mentioned vertical arm, wherein, in at least one vertical arm, be furnished with high temperature recuperative heat exchanger, part high-temperature regenerated catalyst while flowing through this interchanger with this interchanger in heat-eliminating medium carry out heat exchange and make self temperature reduction, and the heat exchange product being produced by heat-eliminating medium, use as superheated vapour can be used as the stripping gas of catalyzer in technique; Meanwhile, at least to maintain current state constant for the vertical arm of another root, and another part high-temperature regenerated catalyst is directly by this arm, and do not carry out cooling.
Regenerated catalyst from different arms mixes near the junction of described arm and conduit (meet), wherein, there is the catalyst temperature of the arm of interchanger to be starkly lower than the catalyst temperature from other arm from internal layout, these regenerated catalysts also conduct heat in the time mixing, thereby, make the temperature of these catalyzer finally approach consistent, like this, the temperature of regenerated catalyst in the time entering described reactor can be starkly lower than the temperature of regenerated catalyst while leaving revivifier (regenerative combustion stove), and, the temperature head of the two can be by regulating the opening degree of above-mentioned vertical arm catalyst stream control valve and the load of high temperature recuperative heat exchanger to adjust.
Therefore, in the present invention, by regulating the opening degree of described vertical arm catalyst stream control valve and/or the load of recuperative heat exchanger, the adjustable temperature that enters the regenerated catalyst in described reactor, reactor reaction bed temperature is controlled between optimum range, for example 450-480 DEG C, like this, has just improved the olefine selective of catalyzer, slow down the coking and deactivation of catalyst surface, and reduced the regeneration frequency of catalyzer.
System of the present invention and technique have the following advantages:
(1) reduce temperature when regenerated catalyst enters reactor, thereby also reduced the coking amount on regenerated catalyst surface;
(2) recuperative heat exchanger can produce high temperature heat exchange product, for example superheated vapour, and its stripping gas that can be used as catalyzer in technique uses;
(3) by regulating the opening degree of described arm catalyst stream control valve and/or the load of recuperative heat exchanger, temperature when adjustable regenerated catalyst enters reactor, reactor reaction bed temperature is controlled in optimum range, thereby, improve the olefine selective of catalyzer, slow down catalyst surface coking, reduce the regeneration frequency of catalyzer, improve the work-ing life of catalyzer;
(4) optimize the thermal equilibrium of reactor, reduced the load of interchanger in reactor, improved the thermo-efficiency of whole system;
(5) temperature that can flexible reactor, maintain to greatest extent reactor assembly steadily and optimum regime move;
(6) can be according to reactor assembly running condition and market the demand to olefin product kind, according to thermodynamics of reactions and dynamic law, control flexibly the catalyst temperature turning back in reactor, obtain required product composition.
Below, by exemplary and non-limiting specific embodiment is explained the present invention in further detail, so that those of ordinary skill in the art are expressly understood essence of the present invention and marrow more.
Embodiment
Embodiment 1
Carry out the transformation reaction of methanol-to-olefins (MTO) by the system shown in Fig. 1, wherein, flow into the throughput ratio of the high-temperature regenerated catalyst in two vertical arms of revivifier (regenerative combustion chamber) bottom by adjusting, control regenerated catalyst and turn back to the temperature in reactor.
Open internal layout and have the catalyst stream control valve on the arm of recuperative heat exchanger, the part inflow internal layout of the high-temperature regenerated catalyst that flows out revivifier (regenerative combustion chamber) is had in the arm of recuperative heat exchanger, and carry out cooling by recuperative heat exchanger to this part high-temperature regenerated catalyst.
Temperature by this part cooling high-temperature regenerated catalyst of recuperative heat exchanger is reduced to approximately 400 DEG C by 650 DEG C, regulate the quantity of this part catalyzer, make it as 40% of regenerated catalyst total amount, like this, the temperature that regenerated catalyst enters in reactor is about 530 DEG C.
After tested, in the present embodiment 1, the interchanger load reduction in reactor is more than 50%; The instantaneous coke content that catalyzer enters reactor is 1.0wt%, and catalyzer has between the active zone of good olefine selective increases approximately 9%, and the olefin yield of unit catalyzer improves approximately 9%, and catalyst regeneration number of times reduces, extend work-ing life; Because reactor operates at the temperature that is more applicable to conversion of olefines, olefine selective increases, and diene (ethene and propylene) selectivity increases by 1.0%, and diene (ethene and propylene) output increases approximately 1.7%.
Above-mentioned experimental result is illustrated in table 1 below.
Embodiment 2
Carry out the transformation reaction of methyl alcohol (MTO) alkene processed by the system shown in Fig. 1, wherein, turn back to the temperature in reactor by regulating the heat exchange of the recuperative heat exchanger of arranging in above-mentioned arm to load to control regenerated catalyst.
Open internal layout and have the catalyst stream control valve on the arm of recuperative heat exchanger, the part inflow internal layout of the high-temperature regenerated catalyst that flows out revivifier (regenerative combustion chamber) is had in the arm of recuperative heat exchanger, and carry out cooling by recuperative heat exchanger to this part high-temperature regenerated catalyst.
Regulate the flow of heat-eliminating medium in recuperative heat exchanger, progressively strengthen cooling load, make in recuperative heat exchanger, to carry out cooling from a part for the high-temperature regenerated catalyst of revivifier (regenerative combustion chamber), temperature by this part cooling high-temperature regenerated catalyst of recuperative heat exchanger drops to 500 DEG C by 650 DEG C, control the quantity of this part regenerated catalyst, make it as 50% of regenerated catalyst total amount, like this, the temperature that regenerated catalyst enters in reactor is about 575 DEG C.
After tested, in the present embodiment 2, the interchanger load reduction 40% in reactor; The instantaneous coke content that catalyzer enters reactor is 1.2%, and catalyzer has between the active zone of good olefine selective increases approximately 5%, and the olefin yield of unit catalyzer improves approximately 5%, and the regeneration times of catalyzer reduces, extend work-ing life; Because reactor operates at the temperature that is more applicable to conversion of olefines, olefine selective increases, and diene (ethene and propylene) selectivity increases by 1.0%, and diene (ethene and propylene) output increases approximately 1.5%.
Comparative example 1
There is catalyst stream control valve on the arm of recuperative heat exchanger except closing internal layout so that all high-temperature regenerated catalysts are not all arranged the arm of recuperative heat exchanger through another inside, repeat the process of embodiment 1.
After tested, the temperature that regenerated catalyst enters in reactor is about 650 DEG C, and the instantaneous coke content that regenerated catalyst enters reactor is 1.4 % by weight.
Above-mentioned experimental result is illustrated in table 1 below.
Table 1
As can be seen from Table 1: system of the present invention with technique (embodiment 1 and 2) compared with prior art (comparative example 1), the temperature that regenerated catalyst enters in reactor obviously reduces, cause catalyst surface moment coking rate greatly to decline, and brought thus the useful improvement of system, especially reactor processing property and many parameters.
The term that this specification sheets is used and form of presentation are only used as descriptive and nonrestrictive term and form of presentation, in the time using these terms and form of presentation, are not intended to any equivalent exclusion of the feature representing and describe or its integral part.
Although represented and described several embodiment of the present invention, the present invention is not restricted to described embodiment.On the contrary, those of ordinary skill in the art should recognize in the situation that not departing from principle of the present invention and spirit can carry out any accommodation and improvement to these embodiments, and protection scope of the present invention is determined by appended claim and equivalent thereof.
Claims (10)
1. a system that reduces the organic oxygen-containing compound alkene processed of catalyzer coking, comprising:
At least one reactor, organic oxygen-containing compound is converted into alkene therein;
At least one revivifier, decaying catalyst is reproduced by burning therein;
At least one decaying catalyst transport pipe, decaying catalyst is entered in described revivifier by described reactor through described pipeline;
At least one regenerated catalyst road, regenerated catalyst is entered in described reactor by described revivifier through described pipeline, described regenerated catalyst road comprises at least two arms near the part of described revivifier, part near described reactor comprises at least one conduit, and described arm and described conduit are interconnected;
Wherein, in above-mentioned at least one arm, there is at least one indirect heat exchanger, for the cooling regenerated catalyst that enters this arm, cooled regenerated catalyst mixes with the regenerated catalyst from other arm at the connecting zone place of described arm and described conduit, and enter in above-mentioned reactor through described conduit, so prevent from entering regenerated catalyst temperature in described reactor too high when preventing that regenerated catalyst from contacting in described reactor with organic oxygen-containing compound surface by fast charring.
2. system according to claim 1, wherein, described organic oxygen-containing compound is methyl alcohol and/or dme; Described alkene is low-carbon alkene; Described catalyzer is SAPO-34, SAPO-18 and/or SAPO-100 catalyzer.
3. system according to claim 1, wherein, described revivifier is vertical type combustion chamber; Described indirect heat exchanger is recuperative heat exchanger; Described arm is vertical; Described indirect heat exchanger is that vertical, level or inclination are arranged.
4. system according to claim 1, wherein, described system also comprises: regenerated catalyst flowrate control valve, fluidizing agent medium entry pipe, fluidizing agent rate-of flow and/or pressure controlled valve and/or temperature monitoring and control device.
5. system according to claim 4, wherein, described temperature monitoring and control device are for monitoring and control described reactor, revivifier, arm and conduit, indirect heat exchanger and the regenerated catalyst temperature at different positions place.
6. system according to claim 5, wherein, described temperature monitoring and control device regulate temperature automatically according to the result of monitoring, make it within rational scope.
7. system according to claim 1, wherein, by regulating the opening degree of regenerated catalyst flowrate control valve and the load of indirect type interchanger to regulate the regenerated catalyst temperature entering in above-mentioned reactor reaction bed, be 450-480 DEG C thereby make the temperature of described reactor reaction bed.
8. system according to claim 1 wherein, is accounted for the 10-60% of regenerated catalyst total amount described at least one by the cooling regenerated catalyst of indirect heat exchanger described at least one in arm; The temperature that enters the regenerated catalyst in above-mentioned reactor is 500-625 DEG C.
9. the technique by organic oxygen-containing compound alkene processed by one of any described system of claim 1-8, comprising:
(1) in described reactor, pass into organic oxygen-containing compound, organic oxygen-containing compound, under the effect of catalyzer, is converted into the reaction product that comprises alkene;
(2) above-mentioned reaction product is discharged to reactor, and carry out subsequently product separation, thereby obtain alkene;
(3) decaying catalyst is moved in described revivifier by described reactor by described decaying catalyst transport pipe, decaying catalyst is reproduced by burning in described revivifier;
(4) regenerated catalyst is moved in described reactor by described revivifier by described regenerated catalyst road, continues to participate in reaction,
Wherein, regenerated catalyst is being moved in the process in described reactor by described revivifier, part regenerated catalyst is cooling by indirect heat exchanger described at least one in arm described at least one, cooled regenerated catalyst mixes with the regenerated catalyst from other arm at the connecting zone place of described arm and described conduit, and enter in above-mentioned reactor through described conduit, so prevent from entering regenerated catalyst temperature in described reactor too high when preventing that regenerated catalyst from contacting in described reactor with organic oxygen-containing compound surface by fast charring.
10. technique according to claim 9, wherein, described indirect heat exchanger is cooling-water flowing through straight pipe type or coiled pipe cooler therebetween, this water cooler produces high-temperature steam through heat exchange.
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