CN103387477A - 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 that reduces the organic oxygen-containing compound alkene processed of 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).Usually, the MTO complete set technology is comprised of reaction technology and isolation technique.Reaction technology is designed to core with catalyst preparation and reactor development, take methyl alcohol as the olefin production mixture; Product distributes and purity requirement is the basis of exploitation separating technology.
At first the 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 take 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, and a small amount of carbon deposit reaction is also arranged.
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 needs coke burning regeneration in fluid bed regenerator, then, returns to fluidized-bed reactor and continues reaction.Reactor and revivifier all are provided with heat-transfering device.
It is the technique of low-carbon alkene through methanol conversion that MTO is actually by synthetic gas.Some famous oil and chemical companies in the world, all drop into substantial contribution and personnel as Exxon Mobil Corporation (Exxon – Mobil), BASF AG (BASF), AP Oil company (UOP) and Hydro company (Norsk Hydro), carried out years of researches.
It is reported, the MTO process products of UOP/Hydro forms comparatively simple, and dopant species and content are less, realizes that more easily product separation reclaims, and can adjust C in reaction product in relative broad range
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 the 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 that is arranged in reactor and revivifier.Decaying catalyst in revivifier the temperature after coke burning regeneration up to 600-700 ℃; although being installed in revivifier, interchanger reduces 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 ℃.Organic oxygen-containing compound, for example methyl alcohol are heated to 160-170 ℃ before entering reactor, comparatively speaking, cold methanol gas is after running into suddenly very hot catalyzer, will be at the catalyst surface fast charring, small duct and the active sites of the coke meeting blocking catalyst that generates, 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 ℃, temperature is that the high temperature catalyst of 630-650 ℃ enters that to participate in thermal discharge after reactor be the conversion reaction of 37-53kJ/mol, on the one hand methyl alcohol is with after catalyzer contacts, catalyst surface can, because of high temperature carbonization coking rapidly, cause 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 the reactor.
For this reason, some investigators have set about studying and how have suitably reduced the temperature that enters the regenerated catalyst in reactor, to reduce the too fast coking of catalyst surface, also guarantee whereby the technical problem of catalyst activity.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, this regenerated granule is mixed with the particle that has in its surface coke so that the mode that their catalytic activity remains on predeterminated level, thereby guarantee 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 take the molecular screen material in this regenerated catalyst particles as benchmark, coke content is less than about 1wt%; (2) at the temperature less than 550 ℃, with this regenerated catalyst particles with contain the coking catalyst particle of 2wt% coke at least and mix; (3) regenerated catalyst particles is mixed with the coking catalyst particle at the temperature of about 400-550 ℃; (4) regenerated catalyst particles be cooled before the coking catalyst particle mixes.
In aforesaid method; although regenerated catalyst is cooled and in the coking catalyst particle, realize mechanically mixing; but the coking catalyst particle is not regeneration; and the coke on this part granules of catalyst is difficult to transfer to above coke content regenerated catalyst particles seldom 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 the catalyst surface coking and guaranteeing that whereby the effect of catalyst activity is limited.
CN1007784B discloses a kind of fluidized particles regeneration and the cooling method and apparatus that carries out simultaneously.It is actually a kind of hot particle of solid combustible (as the catalyzer in the 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 with circulating cooling medium and cooling in the vertical shell-and-tube interchanger.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 the interchanger fluidized-bed layer.Interchanger is in the bottom of cooling room, imports and exports conduit lower than hot particle fully.Therefore, maintenance can be shifted out interchanger during cooling room, and the pipe of interchanger is embedded in the cold granules of catalyst of fluidisation not, thereby reaches the purpose of protection heat exchanger tube.The fluidized gas that comes from interchanger is introduced in the combustion zone, bottom as auxiliary source of the gas, to guarantee sufficient combustion.
In aforesaid method and device, described interchanger is the back-mixing interchanger, be that cooling hot particle, for example granules of catalyst got back in combustion chamber as moving thermal medium again, the temperature that is used for the control combustion chamber, and then control the temperature of the hot particle of part that does not enter in interchanger and directly 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 through burning, regenerating.
Therefore, when the granules of catalyst of organic oxygen-containing compound alkene processed was in entering reactor, excess Temperature caused the problem of the rapid coking of catalyst surface, in the urgent need to a kind of practicality and easy terms of settlement are arranged.
The present invention is intended to solve the insoluble technical problem of this prior art, and proposes a kind of system and technique thereof that reduces the organic oxygen-containing compound alkene processed of catalyzer coking.
Summary of the invention
According to a first aspect of the invention, provide a kind of system that reduces the organic oxygen-containing compound alkene processed of catalyzer coking, comprising:
At least one reactor, organic oxygen-containing compound are converted into alkene therein;
At least one revivifier, decaying catalyst are 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, has at least one indirect heat exchanger in above-mentioned at least one arm, be used 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 the 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 used for monitoring and control described reactor, revivifier, arm and conduit, indirect heat exchanger and the regenerated catalyst temperature at the different positions place, more preferably, described temperature monitoring and control device are regulated temperature automatically according to the result of monitoring, within making it to be in rational scope.
More preferably, in said system, regulating by the opening degree of adjusting regenerated catalyst flowrate control valve and the load of indirect type interchanger the regenerated catalyst temperature that enters in above-mentioned reactor reaction bed, is 450-480 ℃ thereby make the temperature of described reactor reaction bed.Concrete way is: the 10-60% that is accounted for the regenerated catalyst total amount at least one described arm by the cooling regenerated catalyst of at least one described indirect heat exchanger; The temperature that enters the regenerated catalyst in above-mentioned reactor is 500-625 ℃.
According to a second aspect of the invention, provide a kind of with the technique of said system by organic oxygen-containing compound alkene processed, comprising:
(1) pass into organic oxygen-containing compound in described reactor, 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 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, the sustainable participation reaction,
Wherein, in the process of regenerated catalyst in by described revivifier, moving to described reactor, part regenerated catalyst is cooling by at least one described indirect heat exchanger at least one described 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, in above-mentioned technique, described indirect heat exchanger is cooling-water flowing through therebetween straight pipe type or coiled pipe cooler, 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.
Description of drawings
The Figure of description that forms a specification sheets part of the present invention is used for the present invention is further explained; accompanying drawing of the present invention and explanation thereof are used for explaining in detail the present invention; so that those of ordinary skills 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 following description only is used for making the general technical staff of the technical field of the invention can more be expressly understood principle of the present invention and marrow, and does not mean that the present invention is carried out any type of restriction.
Usually, the conversion reaction of organic oxygen-containing compound alkene processed, for example MTO reaction show as the one-level rapid reaction on fresh ASPO-34 catalyst surface, catalyzer has best organic oxygen-containing compound when coke content is the 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: by burning, catalyst regeneration is approximately turned back to catalyzer in reactor during 1.5 % by weight and participates in reaction, carries out coke burning regeneration in after coke content is greater than 5.0 % by weight, catalyzer being entered revivifier from reactor to containing charcoal in revivifier.Reduce when high-temperature regenerated catalyst turns back in reactor as far as possible and 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 at least two vertical arms of root regeneration merge at least one delivery conduit before entering reactor, enter in reactor after mixing near meet from the regenerated catalyst of different arms to participate in organic oxygen-containing compound conversion of olefines processed and react.
Specifically, as shown in Figure 1, the high temperature catalyst after regeneration flows in two vertical arms for delivery of regenerated catalyst simultaneously at least.Usually, be provided with the catalyst stream control valve in above-mentioned vertical arm regenerated catalyst ingress and regulate catalyst amounts in entering above-mentioned vertical arm, wherein, be furnished with the high temperature recuperative heat exchanger at least one vertical arm, part high-temperature regenerated catalyst while flowing through this interchanger with this interchanger in heat-eliminating medium carry out heat exchange self temperature reduced, and the heat exchange product that is produced by heat-eliminating medium, the stripping gas use that can be used as catalyzer in technique as superheated vapour; Simultaneously, to keep current state constant for the vertical arm of another root at least, and namely 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 catalyst temperature from other arm from internal layout, these regenerated catalysts also conduct heat when mixing, thereby, make the temperature of these catalyzer finally approach consistent, like this, the temperature of regenerated catalyst when entering described reactor can be starkly lower than the temperature of regenerated catalyst while leaving revivifier (regenerative combustion stove), and, temperature head both can be by regulating above-mentioned vertical arm catalyst stream control valve opening degree and the load of high temperature recuperative heat exchanger adjust.
Therefore, in the present invention, opening degree by regulating described vertical arm catalyst stream control valve and/or the load of recuperative heat exchanger, can regulate the temperature that enters the regenerated catalyst in described reactor, the reactor reaction bed temperature is controlled between optimum range, for example 450-480 ℃, 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 the opening degree of the described arm catalyst stream control valve of adjusting and/or the load of recuperative heat exchanger, temperature in the time of can regulating regenerated catalyst and enter reactor, the reactor reaction bed temperature is controlled in optimum range, thereby, improve the olefine selective of catalyzer, slow down the 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 the reactor, improved the thermo-efficiency of whole system;
(5) but the temperature of flexible reactor, keep to greatest extent reactor assembly steadily and optimum regime move;
(6) can, according to thermodynamics of reactions and dynamic law, control flexibly the catalyst temperature that turns back in reactor according to reactor assembly running condition and the market demand to the olefin product kind, obtain required product and form.
Below, explain in further detail the present invention by exemplary and nonrestrictive specific embodiment, so that those of ordinary skills are expressly understood essence of the present invention and marrow more.
Embodiment
Embodiment 1
Carry out the transformation reaction of methanol-to-olefins (MTO) with system shown in Figure 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 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 by recuperative heat exchanger, to this part high-temperature regenerated catalyst, carry out cooling.
Temperature by this part cooling high-temperature regenerated catalyst of recuperative heat exchanger is reduced to approximately 400 ℃ by 650 ℃, 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 ℃.
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 the catalyst regeneration number of times reduces, extend work-ing life; Because reactor operates at the temperature that more is fit 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 following table 1.
Embodiment 2
Carry out the transformation reaction of methyl alcohol (MTO) alkene processed with system shown in Figure 1, wherein, load to control regenerated catalyst by the heat exchange of regulating the recuperative heat exchanger of arranging in above-mentioned arm and turn back to 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 by recuperative heat exchanger, to this part high-temperature regenerated catalyst, carry out cooling.
Regulate the flow of heat-eliminating medium in recuperative heat exchanger, progressively strengthen cooling load, make and carry out cooling in recuperative heat exchanger from the part of 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 ℃ by 650 ℃, 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 ℃.
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 more is fit 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%.
The comparative example 1
Have except closing internal layout on the arm of recuperative heat exchanger the catalyst stream control valve so that all high-temperature regenerated catalysts all through another inside, do not arrange the arm of recuperative heat exchanger, repeat the process of embodiment 1.
After tested, the temperature that regenerated catalyst enters in reactor is about 650 ℃, and the instantaneous coke content that regenerated catalyst enters reactor is 1.4 % by weight.
Above-mentioned experimental result is illustrated in following table 1.
Table 1
As can be seen from Table 1: system of the present invention is compared with prior art (comparative example 1) with technique (embodiment 1 and 2), the temperature that regenerated catalyst enters in reactor obviously reduces, cause catalyst surface moment coking rate greatly to descend, 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 only are used as descriptive and nonrestrictive term and form of presentation, are not intended to the feature that will represent and describe or any equivalent exclusion of its integral part when using these terms and form of presentation.
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 skills should recognize that in the situation that do not break away from principle of the present invention and spirit can be carried out any accommodation and improvement to these embodiments, protection scope of the present invention is determined by appended claim and equivalent thereof.
Claims (10)
1. system that reduces the organic oxygen-containing compound alkene processed of catalyzer coking comprises:
At least one reactor, organic oxygen-containing compound are converted into alkene therein;
At least one revivifier, decaying catalyst are 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, has at least one indirect heat exchanger in above-mentioned at least one arm, be used 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 the 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 used for monitoring and control described reactor, revivifier, arm and conduit, indirect heat exchanger and the regenerated catalyst temperature at the different positions place.
6. system according to claim 5, wherein, described temperature monitoring and control device are regulated temperature automatically according to the result of monitoring, within making it to be in rational scope.
7. system according to claim 1, wherein, regulating by the opening degree of adjusting regenerated catalyst flowrate control valve and the load of indirect type interchanger the regenerated catalyst temperature that enters in above-mentioned reactor reaction bed, is 450-480 ℃ thereby make the temperature of described reactor reaction bed.
8. system according to claim 1, wherein, accounted for the 10-60% of regenerated catalyst total amount by the cooling regenerated catalyst of at least one described indirect heat exchanger at least one described arm; The temperature that enters the regenerated catalyst in above-mentioned reactor is 500-625 ℃.
9. one kind with the technique of one of any described system of claim 1-8 by organic oxygen-containing compound alkene processed, comprising:
(1) pass into organic oxygen-containing compound in described reactor, 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 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, the sustainable participation reaction,
Wherein, in the process of regenerated catalyst in by described revivifier, moving to described reactor, part regenerated catalyst is cooling by at least one described indirect heat exchanger at least one described 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.
10. technique according to claim 9, wherein, described indirect heat exchanger is cooling-water flowing through therebetween straight pipe type or coiled pipe cooler, this water cooler produces high-temperature steam through heat exchange.
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| CN107899519A (en) * | 2017-11-02 | 2018-04-13 | 中石化炼化工程（集团）股份有限公司 | A kind of method of system and preparing low-carbon olefin for F- T synthesis |
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