CN204474555U - A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons - Google Patents
A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons Download PDFInfo
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- CN204474555U CN204474555U CN201520058029.5U CN201520058029U CN204474555U CN 204474555 U CN204474555 U CN 204474555U CN 201520058029 U CN201520058029 U CN 201520058029U CN 204474555 U CN204474555 U CN 204474555U
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Abstract
The utility model discloses a kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons, this system comprises reactor (1) and revivifier (2); It is characterized in that, described reactor (1) comprises the reactor dilute phase section (4) and dense-phase bed conversion zone (3) that are communicated with up and down, and described reactor dilute phase section (4) is positioned at the top of described dense-phase bed conversion zone (3); Described revivifier (2) comprises the first revivifier (5) and Second reactivator (6).Adopt system of the present utility model to prepare aromatic hydrocarbons, not only process safety is steady, can realize operate continuously, and can reduce and burn by oxygen-containing gas consumption and catalyst stack less and hydrothermal deactivation, and running cost is low and environmental pollution is little.
Description
Technical field
The utility model relates to a kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons.
Background technology
Aromatic hydrocarbons is a kind of important organic chemical industry's basic material, wherein benzene, toluene and dimethylbenzene (comprising o-Xylol, m-xylene and p-Xylol) purposes are very extensive, and its end product is for the synthesis of resin, synthon, synthetic rubber, coating, dyestuff and medicine and other fields.Along with China's socio-economic development, also growing to the demand of aromatic hydrocarbons, the consumption of the annual aromatic hydrocarbons of current China more than 2,000 ten thousand tons, but has half need from external import.
Benzene, toluene and dimethylbenzene are mainly derived from petrochemical industry, the aromatic hydrocarbons that domestic petroleum chemical industry route is produced accounts for aromatics production total amount more than 85%, production technology mainly comprises: Naphtha reformation, the extracting of cracking of ethylene petroleum naphtha hydrogenation and low-carbon (LC) aromatization of hydrocarbons etc., wherein Naphtha reformed arene output accounts for 80% of petrochemical complex route aromatic production, and cracking of ethylene petroleum naphtha hydrogenation extracting aromatic production accounts for 16%.Along with the exhaustion day by day of petroleum resources, crude oil price remains high, and brings larger cost pressure to petrochemical complex route preparing aromatic hydrocarbon.The Energy Situation of China is the few oily deficency of many coals, with economic sustainable growth since the nineties in 20th century, China's external oil dependency degree constantly increases, 1993 to 1996, China's external oil dependency degree, substantially within 10%, by 2000 first more than 30%, reaches 50.5% in 2007, within 2013, reach 57.39%, far exceed 30% barrier line of generally acknowledging in the world.Then, rich coal resources in China, in recent years under national policy is supported, the industries such as ammonia from coal, dme and ethylene glycol develop rapidly, according to statistics nearly 2,900 ten thousand tons of China's methanol output in 2013.Therefore, development organic oxygen compound catalytic cracking aromatic hydrocarbons technology, to substitute traditional petrochemical complex route, can reduce the dependency degree of aromatic hydrocarbons to petroleum, have important effect to Chinese energy safety and aromatics production industry.
Utilize the technology of organic oxygen compound catalytic cracking aromatic hydrocarbons, proposed the earliest by Mobil Oil Corp. of the U.S., the patent US4156698 A of application in its 1979 discloses and utilizes the composite catalyst containing molecular sieve by C
1-C
4alcohols or ether compound are converted into the method for low-carbon alkene and aromatic hydrocarbons; Disclosing in the patent US4590321A of application in 1985 utilizes ZSM-5 or ZSM-11 equimolecular sieve catalyst by C
2-C
12alkane, C
2-C
12alkene, C
1-C
5alcohols and C
2-C
12the non-aromatics converting compounds such as ethers are the technique of aromatic hydrocarbons; US Patent No. 4686312 A, US4724270 A, US4822939 A, US4822939 A and US4049573 A etc. also discloses the method for methyl alcohol or dimethyl ether aromatic hydrocarbons under different catalysts effect.But the emphasis of these United States Patent (USP)s is mainly that Study of Catalyst composition and operation condition are on aromatics conversion rate with optionally affect, indivedual patent proposes the reaction process of methyl alcohol or dimethyl ether aromatic hydrocarbons, but does not all clearly propose the reaction-regeneration system of organic oxygen compound aromatic hydrocarbons technology, reaction regeneration method and reactor and revivifier pattern.
At present, domestic Ye Youduojia institute researches and develops organic oxygen compound aromatic hydrocarbons technology, mainly comprises Tsing-Hua University, Shanxi Inst. of Coal Chemistry, Chinese Academy of Sciences, Sinopec Shanghai Petroleum Chemical Engineering Institute and Dalian Inst of Chemicophysics, Chinese Academy of Sciences etc.It is the technique of raw material aromatic hydrocarbons processed under ZSM-5 Type Zeolites agent effect that Chinese patent CN 1880288A discloses with methyl alcohol, this patent isolates low-carbon (LC) hydro carbons and liquid product after being cooled by first stage reactor aromatization of methanol gas-phase product, liquid product obtains aromatic hydrocarbons and non-aromatics through extracting and separating, low-carbon (LC) hydro carbons enters the further aromizing of second stage reactor, thus improves the overall selectivity of aromatic hydrocarbons.Chinese patent CN 101823929 B proposes system and the technique of a kind of methyl alcohol or dme preparing aromatic hydrocarbon, and methyl alcohol or dme first react at aromatization reactor, hydrogen, methane, mixed C in reaction product
8aromatic hydrocarbons and part C
9+hydro carbons as product, C
2+non-aromatics and except mixed C
8aromatic hydrocarbons and part C
9+aromatic hydrocarbons outside hydro carbons then can be recycled to another reactor and carry out further aromizing, improves yield and the selectivity of aromatic hydrocarbons.Chinese patent CN 101607858 B, CN 102190546B, CN 102371176 B and CN 102371177 B etc. also individually disclose organic oxygen compound catalytic cracking aromatics process and the arenes catalytic agent of organic oxygen compound catalytic cracking and preparation method.Above-mentioned patent focus on equally investigate different catalysts composition and rare metal, the rare-earth metal modified impact on aromatization process, CN 1880288A and CN 101823929 B mainly proposes reaction product circulation aromizing to the impact of aromatics yield, but these patents do not relate to the reaction-regeneration system of organic oxygen compound aromatic hydrocarbons yet.
Chinese patent CN 101244969 A discloses the devices and methods therefor of a kind of continuous aromatization and catalyst regeneration, this device comprises the fluidized-bed of an aromizing fluidized-bed and a continuous catalyst regenerating and the pipeline for catalyst transport be arranged between two fluidized-beds and solids delivery device, but this patent does not propose the specific form of regeneration system rapidly, and there are some problems: revivifier only establishes one-level gas solid separation system, catalyst recovery yield is low, causes expensive catalyst stack less serious; Revivifier pattern is the regeneration of single hop bed, and for ensureing catalyst regeneration efficiency, regeneration temperature reaches as high as 750 DEG C, owing to containing part hydrogen in the coke of catalyst entrainment, generate water after burning, under high temperature and water vapor acting, catalyzer hydrothermal deactivation is serious, causes catalyst activity to reduce; Revivifier heat-obtaining mode is interior heat-obtaining, and only arranges a heat production coil pipe, and when coil pipe bursts, heat-obtaining medium scurries into revivifier in a large number, regenerator pressure can be caused to raise rapidly, even can set off an explosion time serious.
Utility model content
The purpose of this utility model is to provide a kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons, this system can meet raising aromatic hydrocarbon product yield and optionally requirement, be suitable for again organic oxygen compound catalytic cracking arene industrial continuous seepage, can significantly reduce catalyst stack less and hydrothermal deactivation simultaneously, reduce the cost of industrialization organic oxygen compound catalytic cracking aromatic hydrocarbons.
To achieve these goals, the utility model provides a kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons, and this system comprises reactor 1 and revivifier 2; It is characterized in that, described reactor 1 comprises the reactor dilute phase section 4 and dense-phase bed conversion zone 3 that are communicated with up and down, and described reactor dilute phase section 4 is positioned at the top of described dense-phase bed conversion zone 3; The bottom of described dense-phase bed conversion zone 3 is provided with the feed distributing plate 10 for the described organic oxygen compound sending into described dense-phase bed conversion zone 3 that distributes, and described feed distributing plate 10 is positioned at the below of the regenerant inlet of described dense-phase bed conversion zone 3 bottom; Described revivifier 2 comprises the first revivifier 5 and Second reactivator 6; The spent agent outlet on described dense-phase bed conversion zone 3 top is communicated with the spent agent entrance on described first revivifier 5 top, the semi regeneration agent outlet of described first revivifier 5 bottom is communicated with the semi regeneration agent entrance of described Second reactivator 6 bottom, and the regenerator outlet of described Second reactivator 6 is communicated with the described regenerant inlet of described dense-phase bed conversion zone 3 bottom.
Preferably, it is characterized in that, in described reactor dilute phase section 4, be provided with at least one group of reactor primary cyclone 11 and reactor secondary cyclone 12 of mutually contacting.
Preferably, it is characterized in that, the described spent agent outlet on described dense-phase bed conversion zone 3 top is communicated with the spent agent stripper 7 for stripping spent agent entrained with oil gas by inclined tube on spent agent 14; Described spent agent stripper 7 is communicated with the described spent agent entrance on described first revivifier 5 top by spent agent lower oblique tube 16, or is communicated with the described spent agent entrance of spent agent riser tube 18 with described first revivifier 5 top by spent agent lower oblique tube 16 successively; Described spent agent lower oblique tube 16 is provided with the guiding valve to be generated 17 for controlling described reactor 1 catalyzer material level; Bottom in described spent agent stripper 7 cavity is provided with the stripping fluid distribution pipe 15 for being uniformly distributed the stripping fluid sending into described spent agent stripper 7.
Preferably, it is characterized in that, bottom in described first revivifier 5 cavity is provided with the oxygen-containing gas distribution rings 20 for being uniformly distributed the regeneration oxygen-containing gas sending into described first revivifier 5, and the bottom in Second reactivator 6 cavity is provided with the oxygen-containing gas distribution pipe 19 for being uniformly distributed the regeneration oxygen-containing gas sending into described Second reactivator 6.
Preferably, it is characterized in that, the top of described first revivifier 5 is set to dilute-phase leanphase fluidized bed section, and bottom is set to dense bed section; The described spent agent entrance on described first revivifier 5 top is positioned at the bottom of the described dilute-phase leanphase fluidized bed section of described first revivifier 5; At least one group of the first revivifier primary cyclone 21 and the first revivifier secondary cyclone 22 of mutually contacting is provided with in the described dilute-phase leanphase fluidized bed section of described first revivifier 5.
Preferably, it is characterized in that, described first revivifier 5 and described Second reactivator 6 are for overlap up and down, and the exhanst gas outlet at described Second reactivator 6 top is communicated with by low pressure drop grid distributor with the bottom of described first revivifier 5.
Preferably, it is characterized in that, the described semi regeneration agent outlet of described first revivifier 5 is communicated with the semi regeneration deaeration pipe 9 for removing semi regeneration catalyzer entrained with flue gas by inclined tube on semi regeneration 28; Described semi regeneration deaeration pipe 9 is communicated with the described semi regeneration agent entrance of described Second reactivator 6 by semi regeneration lower oblique tube 30; Described semi regeneration lower oblique tube 30 is provided with the semi regeneration guiding valve 31 for controlling described first revivifier 5 catalyzer material level; Bottom in described semi regeneration deaeration pipe 9 cavity is provided with the degassed dielectric distribution ring 29 of semi regeneration agent for being uniformly distributed the degassed medium of semi regeneration agent sending into described semi regeneration deaeration pipe 9.
Preferably, it is characterized in that, described first revivifier 5 is with described Second reactivator 6 for being set up in parallel, and the top of described Second reactivator 6 is set to dilute-phase leanphase fluidized bed section, and bottom is set to dense bed section; The described semi regeneration agent entrance of described Second reactivator 6 bottom is positioned at the bottom of the dense bed section of described Second reactivator 6, and the described regenerator outlet of described Second reactivator 6 is positioned at the top of the dense bed section of described Second reactivator 6; At least one group of Second reactivator primary cyclone 34 and Second reactivator secondary cyclone 35 of mutually contacting is provided with in the dilute-phase leanphase fluidized bed section of described Second reactivator 6.
Preferably, it is characterized in that, described semi regeneration agent outlet bottom described first revivifier 5 is communicated with the described semi regeneration agent entrance of semi regeneration agent riser tube 33 with the bottom of described Second reactivator 6 dense bed section by semi regeneration lower oblique tube 30 successively, or is directly communicated with the described semi regeneration agent entrance of the bottom of described Second reactivator 6 dense bed section by semi regeneration lower oblique tube 30; Described semi regeneration lower oblique tube 30 is provided with the semi regeneration guiding valve 31 for controlling described first revivifier 5 catalyzer material level.
Preferably, it is characterized in that, the described regenerator outlet of described Second reactivator 6 is communicated with the regenerator degassing vessel 8 for removing regenerated catalyst entrained with flue gas by inclined tube on regenerator 24; Described regenerator degassing vessel 8 is communicated with the described regenerant inlet of regenerator riser tube 32 with described dense-phase bed conversion zone 3 bottom by regenerator lower oblique tube 26 successively, or is directly communicated with the regenerant inlet of described dense-phase bed conversion zone 3 bottom by regenerator lower oblique tube 26; Described regenerator lower oblique tube 26 is provided with the regeneration guiding valve 27 for controlling described Second reactivator 6 catalyzer material level; Bottom in described regenerator degassing vessel 8 cavity is provided with the degassed dielectric distribution ring 25 of regenerator for being uniformly distributed the degassed medium of regenerator sending into described regenerator degassing vessel 8.
The system tool of the organic oxygen compound catalytic cracking aromatic hydrocarbons that the utility model provides has the following advantages:
1, the reaction of organic oxygen compound catalytic cracking aromatic hydrocarbons and catalyst regeneration carry out respectively in reactor and revivifier, between two devices, inclined tube all arranges degassed facility, reaction raw materials and product do not contact with oxygen-containing gas substantially with burning, and process safety is steady, can realize operate continuously;
2, two revivifiers are provided with, first revivifier can be set to low temperature oxygen deprivation operation, Second reactivator can be set to high-temperature oxygen-enriched operation, while reducing catalyzer hydrothermal deactivation to the full extent, can reduce to burn and use oxygen-containing gas consumption, thus reduce the running cost of organic oxygen compound catalytic cracking aromatic hydrocarbons;
3, reactor and revivifier all arrange at least one group of two stage cyclone separator, reclaim the catalyzer carried secretly in reaction product and flue gas as far as possible, catalyst attrition and running cost can be reduced, the environmental pollution that the pipeline of the follow-up cooling separation of reaction product and equipment attrition and fume emission bring can also be reduced.
Other feature and advantage of the present utility model are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for specification sheets, is used from explanation the utility model, but does not form restriction of the present utility model with embodiment one below.In the accompanying drawings:
Fig. 1 is the first embodiment (i.e. eclipsed form two-stage regeneration, reclaimable catalyst delivery conduit adopts and promotes wind lifting) of organic oxygen compound catalytic cracking aromatic hydrocarbon system of the present utility model;
Fig. 2 is the second embodiment (i.e. eclipsed form two-stage regeneration, regenerated catalyst delivery conduit adopts and promotes wind lifting) of organic oxygen compound catalytic cracking aromatic hydrocarbon system of the present utility model;
Fig. 3 is the third embodiment (i.e. eclipsed form two-stage regeneration, reclaimable catalyst and regenerated catalyst delivery conduit all adopt and promote wind lifting) of organic oxygen compound catalytic cracking aromatic hydrocarbon system of the present utility model;
Fig. 4 is the 4th kind of embodiment (i.e. block form two-stage regeneration, semi regeneration catalyst transport circuit adopts and promotes wind lifting) of organic oxygen compound catalytic cracking aromatic hydrocarbon system of the present utility model.
Description of reference numerals
1 reactor, 2 revivifiers, 3 dense-phase bed conversion zones, 4 reactor dilute phase section 5 first revivifiers, 6 Second reactivators, 7 spent agent strippers, 8 regenerator degassing vessel 9 semi regeneration deaeration pipes, 10 feed distributing plates, 11 reactor primary cyclone 12 reactor secondary cyclones, 13 reactor collection chambers, inclined tube 15 stripping fluid distribution pipe on 14 spent agents, 16 spent agent lower oblique tubes, 17 guiding valve 18 spent agent riser tubes to be generated, 19 oxygen-containing gas distribution pipes, 20 oxygen-containing gas distribution rings 21 first revivifier primary cyclones, 22 first revivifier secondary cyclone 23 first revivifier collection chambers, inclined tube on 24 regenerators, 25 regenerator degassed dielectric distribution ring 26 regenerator lower oblique tube, 27 regeneration guiding valves, the degassed dielectric distribution ring of inclined tube 29 semi regeneration agent on 28 semi regeneration, 30 semi regeneration lower oblique tubes, 31 semi regeneration guiding valve 32 regenerator riser tubes, 33 semi regeneration agent riser tubes, 34 Second reactivator primary cyclone 35 Second reactivator secondary cyclones, 36 Second reactivator collection chambers
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons, and this system comprises reactor 1 and revivifier 2; It is characterized in that, described reactor 1 comprises the reactor dilute phase section 4 and dense-phase bed conversion zone 3 that are communicated with up and down, and described reactor dilute phase section 4 is positioned at the top of described dense-phase bed conversion zone 3; The bottom of described dense-phase bed conversion zone 3 is provided with the feed distributing plate 10 for the described organic oxygen compound sending into described dense-phase bed conversion zone 3 that distributes, and described feed distributing plate 10 is positioned at the below of the regenerant inlet of described dense-phase bed conversion zone 3 bottom; Described revivifier 2 comprises the first revivifier 5 and Second reactivator 6; The spent agent outlet on described dense-phase bed conversion zone 3 top is communicated with the spent agent entrance on described first revivifier 5 top, the semi regeneration agent outlet of described first revivifier 5 bottom is communicated with the semi regeneration agent entrance of described Second reactivator 6 bottom, and the regenerator outlet of described Second reactivator 6 is communicated with the described regenerant inlet of described dense-phase bed conversion zone 3 bottom.
According to the utility model, described organic oxygen compound and the catalyzer for organic oxygen compound catalytic cracking aromatic hydrocarbons are well known to the skilled person, and such as, described organic oxygen compound can for being selected from C
1-C
10alcohols, C
2-C
12ethers and C
3-C
12at least one in ketone; Described catalyzer can for the microspherical catalyst containing molecular sieve and carrier, and described molecular sieve is preferably ZSM-5 molecular sieve.
According to the utility model, described dense-phase bed conversion zone 3 is dense bed section, reactor dilute phase section 4 is dilute-phase leanphase fluidized bed section, arranging dense bed section is to control the residence time of organic oxygen compound at reaction bed, ensure the abundant high-efficient contact between material benzenemethanol and catalyzer, suppress air pocket and catalyst agglomeration thing to generate, thus maintain higher reaction conversion ratio and arenes selectivity, arranging dilute-phase leanphase fluidized bed section is to make reactor product gas compared with the catalyzer carried secretly by gravity initial gross separation under low flow velocity, and there are enough spatial arrangement two stage cyclone separator for further separation catalyzer, reduce the wearing and tearing to follow-up equipment and pipeline of catalyst stack less and catalyzer, in order to the catalyst inventory that increases in reactor and facilitate the flutter valve of cyclonic separator to be arranged in dense-phase bed to reduce catalyst stack less, in reactor 1, the actual height being in the catalyst layer of dense fluidized state can not have the flutter valve of cyclonic separator, this is well-known to those skilled in the art.When adopting the utility model to carry out aromatization, preferred reaction conditions is as follows: the temperature of reaction of dense-phase bed conversion zone 3 is 400-600 DEG C, the reaction pressure of reactor dilute phase section 4 is 0.05-0.6MPa (g), and dense-phase bed conversion zone mass space velocity is 0.1-10 hour
-1, organic oxygen compound is 5-30 second in the residence time of dense-phase bed conversion zone.But those skilled in the art also can arrange the condition of aromatization according to the needs of real reaction, the utility model is restriction not.
According to the utility model, described reactive system can be provided with at least one group of two stage cyclone separator and carry out being separated of described reaction product and reclaimable catalyst, such as, at least one group of reactor primary cyclone 11 and reactor secondary cyclone 12 of mutually contacting can be provided with in described reactor dilute phase section 4.Described cyclonic separator is well-known to those skilled in the art, and the utility model repeats no more.General one group of two stage cyclone separator comprises a primary cyclone and a secondary cyclone of series connection; When arranging many group two stage cyclone separators, primary cyclone is generally identical with the quantity of secondary cyclone, between can be connected one to one by draft tube, also after the riser of multiple primary cyclone can being merged into a collecting tubule, be connected with multiple secondary cyclone again, the secondary riser of secondary cyclone is all connected with collection chamber, and described collection chamber can be located at the inside of reactor dilute phase section 4, also can be located at the outside of reactor dilute phase section 4.It should be noted that, cyclonic separator described in the utility model revivifier also all can so be arranged, and hereafter will repeat no more.
According to the utility model, reacted reclaimable catalyst can be drawn reactor 1 from inclined tube 14 spent agent on described dense-phase bed conversion zone 3 top, after stripping, be delivered to the first revivifier 5.According to a kind of embodiment of the present utility model, the described spent agent outlet on described dense-phase bed conversion zone 3 top can be communicated with the spent agent stripper 7 for stripping spent agent entrained with oil gas by inclined tube on spent agent 14; Bottom in described spent agent stripper 7 cavity can be provided with the stripping fluid distribution pipe 15 for being uniformly distributed the stripping fluid sending into described spent agent stripper 7.Wherein, the effect of described spent agent stripper 7 is partial reaction products of spent agent entrained with after stripping reaction, to reduce product loss.Can be provided with one or more stripping fluid distribution pipes 15 in described spent agent stripper 7 and be used for the stripping fluid that distributes, described stripping fluid can include but not limited to be selected from least one in steam, nitrogen, methane, dry gas and fuel gas.
Different from the height of the spent agent entrance of the first revivifier 1 according to the spent agent outlet of dense-phase bed conversion zone 3, spent agent has two kinds by dense-phase bed conversion zone 3 to the mode of movement of the first revivifier 5: when the spent agent of dense-phase bed conversion zone 3 export higher than the spent agent entrance of the first revivifier 5 more time, spent agent can by deadweight from flow in the first revivifier 5; When the spent agent outlet of dense-phase bed conversion zone 3 is lower, identical than the first revivifier 5 spent agent entrance or when exceeding few, spent agent can be sent in the first revivifier 5 by promoting wind, namely described spent agent stripper 7 can be communicated with (as shown in Figure 2,4) with the described spent agent entrance on described first revivifier 5 top by spent agent lower oblique tube 16, or can be communicated with (as shown in Figure 1,3) with the described spent agent entrance of spent agent riser tube 18 with described first revivifier 5 top by spent agent lower oblique tube 16 successively; Described spent agent lower oblique tube 16 can be provided with the guiding valve to be generated 17 for controlling described reactor 1 catalyzer material level.Can send into lifting wind in described spent agent riser tube 18, described lifting wind can include but not limited to be selected from least one in oxygen-containing gas, nitrogen and steam.
Contriver of the present utility model finds, organic oxygen compound catalytic cracking arenes catalytic agent hydrothermal deactivation when high temperature and high steam partial pressure is comparatively obvious, therefore the upper and lower arranged superposed of the utility model or be arranged in juxtaposition two revivifiers and two-stage regeneration carried out to reclaimable catalyst, to reduce the high-temperature water heat inactivation of catalyzer.Namely described first revivifier 5 can operate for the oxygen deprivation of employing first oxygen-containing gas, regeneration temperature can be 500-650 DEG C, and the combustionvelocity due to Hydrogen In The Coke is far longer than the combustionvelocity of carbon, under the regeneration condition that reclaimable catalyst comparatively relaxes at the first revivifier, the carbon of the heavy % of 50 heavy %-90 in coke and the protium of the heavy % of 60 heavy %-100 can be burnt, by volume, the first revivifier 5 produce the ratio of carbon monoxide and carbonic acid gas in flue gas can for 0.2-3.Although most of protium can be burnt in the first revivifier 5 become water vapor, lower owing to burning temperature, the hydrothermal deactivation of catalyzer can be effectively reduced.Second reactivator 6 can operate for the oxygen enrichment of employing second oxygen-containing gas, regeneration temperature can be 600-750 DEG C, regeneration condition is harsher than the first revivifier 6, because the basic burning in the first revivifier 5 of Hydrogen In The Coke element is complete, the carbon of the heavy % of 10 heavy %-50 on catalyzer and 0 heavy %-40 can be weighed the protium perfect combustion of % by Second reactivator 6 under the condition of the low steam partial pressure of high temperature, to reduce the hydrothermal deactivation of catalyzer.By volume, Second reactivator 6 produce the content of oxygen in flue gas can for 0.5-15 body %.After described reclaimable catalyst carries out the second regeneration, by weight and with the gross weight of catalyzer for benchmark, in regenerated catalyst, the content of coke can be the heavy % of 0.01-0.1.Certainly, those skilled in the art also can adopt other renovation process to regenerate the agent of organic oxygen compound catalytic cracking arenes catalytic according to practical situation in regeneration system rapidly of the present utility model, and the utility model does not limit.
According to the utility model, for ensureing that regeneration oxygen-containing gas is evenly distributed and fully contacts with catalyzer in the first revivifier 5 with Second reactivator 6, effect and fluidized state is burnt to reach good, bottom in described first revivifier 5 cavity can be provided with the oxygen-containing gas distribution rings 20 for being uniformly distributed the regeneration oxygen-containing gas sending into described first revivifier 5, and the bottom in Second reactivator 6 cavity can be provided with the oxygen-containing gas distribution pipe 19 for being uniformly distributed the regeneration oxygen-containing gas sending into described Second reactivator 6.Wherein, described oxygen-containing gas distribution rings 20 at least should arrange 1 wear resistant short tube; Described oxygen-containing gas distribution pipe 19 generally adopts dendroid distribution pipe, and each dendritic take-off pipe also at least should arrange 1 wear resistant short tube, and therefore the distributed effect of oxygen-containing gas distribution pipe 19 pairs of gases is generally better than oxygen-containing gas distribution rings.
According to the utility model, the top of described first revivifier 5 can be set to dilute-phase leanphase fluidized bed section, bottom can be set to dense bed section, in order to the catalyst inventory that increases in revivifier and facilitate the flutter valve of cyclonic separator to be arranged in dense-phase bed to reduce catalyst stack less, in first revivifier, the actual height being in the catalyst layer of dense fluidized state higher than the height of the spent agent entrance of the first revivifier, can not have the flutter valve of cyclonic separator yet; The described spent agent entrance on described first revivifier 5 top can be positioned at the bottom of the described dilute-phase leanphase fluidized bed section of described first revivifier 5; At least one group of the first revivifier primary cyclone 21 and the first revivifier secondary cyclone 22 of mutually contacting can be provided with in the described dilute-phase leanphase fluidized bed section of described first revivifier 5.
According to the utility model, described first revivifier 5 and described Second reactivator 6 can for overlap up and down, and the exhanst gas outlet at described Second reactivator 6 top can be communicated with by low pressure drop grid distributor with the bottom of described first revivifier 5, as Figure 1-3.Described low pressure drop grid distributor can allow gas to pass through, but only allows a small amount of catalyzer to pass through.The described semi regeneration agent outlet of described first revivifier 5 can be communicated with the semi regeneration deaeration pipe 9 for removing semi regeneration catalyzer entrained with flue gas by inclined tube on semi regeneration 28; Described semi regeneration deaeration pipe 9 can be communicated with the described semi regeneration agent entrance of described Second reactivator 6 by semi regeneration lower oblique tube 30; Described semi regeneration lower oblique tube 30 can being provided with the semi regeneration guiding valve 31 for controlling described first revivifier 5 catalyzer material level, the catalyzer material level of described first revivifier 5 can be controlled by the catalyst stream output controlling described semi regeneration deaeration pipe 9; Bottom in described semi regeneration deaeration pipe 9 cavity can be provided with the degassed dielectric distribution ring 29 of semi regeneration agent for being uniformly distributed the degassed medium of semi regeneration agent sending into described semi regeneration deaeration pipe 9.Described semi regeneration deaeration pipe 9 is well known to those skilled in the art, and its effect is the flue gas reducing semi regeneration catalyst entrainment, increases semi regeneration lower oblique tube 30 inner catalyst density to improve the pressure reduction of semi regeneration guiding valve 31, ensures the quiet run of semi regeneration guiding valve 31.Semi regeneration deaeration pipe 9 can arrange at least 1 degassed dielectric distribution ring 29 of semi regeneration agent, and degassed medium can include but not limited to be selected from least one in steam, nitrogen, air and other rare gas element.
According to the utility model, described first revivifier 5 can for being set up in parallel with described Second reactivator 6, as shown in Figure 4, the top of described Second reactivator 6 can be set to dilute-phase leanphase fluidized bed section, bottom can be set to dense bed section, in order to the catalyst inventory that increases in revivifier and facilitate the flutter valve of cyclonic separator to be arranged on to reduce catalyst stack less in dense-phase bed, in Second reactivator, the actual height being in the catalyst layer of dense fluidized state can not have the flutter valve of cyclonic separator; The described semi regeneration agent entrance of described Second reactivator 6 bottom can be positioned at the bottom of the dense bed section of described Second reactivator 6, and the described regenerator outlet of described Second reactivator 6 can be positioned at the top of the dense bed section of described Second reactivator 6; At least one group of Second reactivator primary cyclone 34 and Second reactivator secondary cyclone 35 of mutually contacting can be provided with in the dilute-phase leanphase fluidized bed section of described Second reactivator 6.
In the utility model, different according to two the revivifier relative levels be set up in parallel, semi regeneration catalyzer can have two kinds by the first revivifier to the mode of movement of Second reactivator: when the bottom of the first revivifier 5 higher than the bottom of Second reactivator 6 more time, described semi regeneration agent outlet bottom described first revivifier 5 can be directly communicated with the described semi regeneration agent entrance of the bottom of described Second reactivator 6 dense bed section by semi regeneration lower oblique tube 30, and semi regeneration catalyzer directly can be flow to the bottom of Second reactivator 6 certainly by deadweight by semi regeneration lower oblique tube 30; When the bottom of the first revivifier 5 lower than the bottom of Second reactivator 6 or identical even slightly high some time, described semi regeneration agent outlet bottom described first revivifier 5 can be communicated with the described semi regeneration agent entrance of semi regeneration agent riser tube 33 with the bottom of described Second reactivator 6 dense bed section by semi regeneration lower oblique tube 30 successively, semi regeneration catalyzer can flow to semi regeneration agent riser tube 33 by semi regeneration lower oblique tube 30, and the lifting wind conveying semi regeneration catalyzer in recycling semi regeneration agent riser tube 33 is to the bottom of Second reactivator 6.In addition, described semi regeneration lower oblique tube 30 can be provided with the semi regeneration guiding valve 31 for controlling described first revivifier 5 catalyzer material level.It should be noted that, in the utility model, " bottom " comprises " bottom ", and namely " the first revivifier 5 bottom " comprises " bottom the first revivifier 5 ".
According to the utility model, the described regenerator outlet of described Second reactivator 6 can be communicated with the regenerator degassing vessel 8 for removing regenerated catalyst entrained with flue gas by inclined tube on regenerator 24.Different from the relative level of reactor according to Second reactivator, described regenerator degassing vessel 8 can be communicated with (as shown in Figure 2,3) with the described regenerant inlet of regenerator riser tube 32 with described dense-phase bed conversion zone 3 bottom by regenerator lower oblique tube 26 successively, or can be directly communicated with the regenerant inlet of described dense-phase bed conversion zone 3 bottom (as shown in Fig. 1,4) by regenerator lower oblique tube 26; Described regenerator lower oblique tube 26 can be provided with the regeneration guiding valve 27 for controlling described Second reactivator 6 catalyzer material level; Bottom in described regenerator degassing vessel 8 cavity can be provided with the degassed dielectric distribution ring 25 of regenerator for being uniformly distributed the degassed medium of regenerator sending into described regenerator degassing vessel 8.For ensureing degasifying effect, the non-hydrocarbon component that minimizing enters in reactor is to reduce reaction product energy consumption of compressor, and regenerator degassing vessel 8 can be provided with at least 1 degassed dielectric distribution ring 25 of regenerator; Described degassed medium can include but not limited to be selected from least one in steam, nitrogen and other rare gas element.
Claims (10)
1. a system for organic oxygen compound catalytic cracking aromatic hydrocarbons, this system comprises reactor (1) and revivifier (2); It is characterized in that, described reactor (1) comprises the reactor dilute phase section (4) and dense-phase bed conversion zone (3) that are communicated with up and down, and described reactor dilute phase section (4) is positioned at the top of described dense-phase bed conversion zone (3); The bottom of described dense-phase bed conversion zone (3) is provided with the feed distributing plate (10) for the described organic oxygen compound sending into described dense-phase bed conversion zone (3) that distributes, and described feed distributing plate (10) is positioned at the below of the regenerant inlet of described dense-phase bed conversion zone (3) bottom; Described revivifier (2) comprises the first revivifier (5) and Second reactivator (6); The spent agent outlet on described dense-phase bed conversion zone (3) top is communicated with the spent agent entrance on described first revivifier (5) top, the semi regeneration agent outlet of described first revivifier (5) bottom is communicated with the semi regeneration agent entrance of described Second reactivator (6) bottom, and the regenerator outlet of described Second reactivator (6) is communicated with the described regenerant inlet of described dense-phase bed conversion zone (3) bottom.
2. system according to claim 1, it is characterized in that, in described reactor dilute phase section (4), be provided with at least one group of reactor primary cyclone (11) and reactor secondary cyclone (12) of mutually contacting.
3. system according to claim 1, it is characterized in that, the described spent agent outlet on described dense-phase bed conversion zone (3) top is communicated with the spent agent stripper (7) for stripping spent agent entrained with oil gas by inclined tube on spent agent (14); Described spent agent stripper (7) is communicated with by the described spent agent entrance of spent agent lower oblique tube (16) with described first revivifier (5) top, or is communicated with the described spent agent entrance of spent agent riser tube (18) with described first revivifier (5) top by spent agent lower oblique tube (16) successively; Described spent agent lower oblique tube (16) is provided with the guiding valve to be generated (17) for controlling described reactor (1) catalyzer material level; Bottom in described spent agent stripper (7) cavity is provided with the stripping fluid distribution pipe (15) for being uniformly distributed the stripping fluid sending into described spent agent stripper (7).
4. system according to claim 1, it is characterized in that, bottom in described first revivifier (5) cavity is provided with the oxygen-containing gas distribution rings (20) for being uniformly distributed the regeneration oxygen-containing gas sending into described first revivifier (5), and the bottom in Second reactivator (6) cavity is provided with the oxygen-containing gas distribution pipe (19) for being uniformly distributed the regeneration oxygen-containing gas sending into described Second reactivator (6).
5. system according to claim 1, is characterized in that, the top of described first revivifier (5) is set to dilute-phase leanphase fluidized bed section, and bottom is set to dense bed section; The described spent agent entrance on described first revivifier (5) top is positioned at the bottom of the described dilute-phase leanphase fluidized bed section of described first revivifier (5); At least one group of the first revivifier primary cyclone (21) and the first revivifier secondary cyclone (22) of mutually contacting is provided with in the described dilute-phase leanphase fluidized bed section of described first revivifier (5).
6. system according to claim 5, it is characterized in that, described first revivifier (5) and described Second reactivator (6) are for overlap up and down, and the exhanst gas outlet at described Second reactivator (6) top is communicated with by low pressure drop grid distributor with the bottom of described first revivifier (5).
7. system according to claim 6, it is characterized in that, the described semi regeneration agent outlet of described first revivifier (5) is communicated with the semi regeneration deaeration pipe (9) for removing semi regeneration catalyzer entrained with flue gas by inclined tube on semi regeneration (28); Described semi regeneration deaeration pipe (9) is communicated with the described semi regeneration agent entrance of described Second reactivator (6) by semi regeneration lower oblique tube (30); Described semi regeneration lower oblique tube (30) is provided with the semi regeneration guiding valve (31) for controlling described first revivifier (5) catalyzer material level; Bottom in described semi regeneration deaeration pipe (9) cavity is provided with the degassed dielectric distribution ring (29) of semi regeneration agent for being uniformly distributed the degassed medium of semi regeneration agent sending into described semi regeneration deaeration pipe (9).
8. system according to claim 5, it is characterized in that, described first revivifier (5) and described Second reactivator (6) are for being set up in parallel, and the top of described Second reactivator (6) is set to dilute-phase leanphase fluidized bed section, and bottom is set to dense bed section; The described semi regeneration agent entrance of described Second reactivator (6) bottom is positioned at the bottom of the dense bed section of described Second reactivator (6), and the described regenerator outlet of described Second reactivator (6) is positioned at the top of the dense bed section of described Second reactivator (6); At least one group of Second reactivator primary cyclone (34) and Second reactivator secondary cyclone (35) of mutually contacting is provided with in the dilute-phase leanphase fluidized bed section of described Second reactivator (6).
9. system according to claim 8, it is characterized in that, the described semi regeneration agent outlet of described first revivifier (5) bottom is communicated with the described semi regeneration agent entrance of semi regeneration agent riser tube (33) with the bottom of described Second reactivator (6) dense bed section by semi regeneration lower oblique tube (30) successively, or is directly communicated with the described semi regeneration agent entrance of the bottom of described Second reactivator (6) dense bed section by semi regeneration lower oblique tube (30); Described semi regeneration lower oblique tube (30) is provided with the semi regeneration guiding valve (31) for controlling described first revivifier (5) catalyzer material level.
10. system according to claim 1, it is characterized in that, the described regenerator outlet of described Second reactivator (6) is communicated with the regenerator degassing vessel (8) for removing regenerated catalyst entrained with flue gas by inclined tube on regenerator (24); Described regenerator degassing vessel (8) is communicated with the described regenerant inlet of regenerator riser tube (32) with described dense-phase bed conversion zone (3) bottom by regenerator lower oblique tube (26) successively, or is directly communicated with the regenerant inlet of described dense-phase bed conversion zone (3) bottom by regenerator lower oblique tube (26); Described regenerator lower oblique tube (26) is provided with the regeneration guiding valve (27) for controlling described Second reactivator (6) catalyzer material level; Bottom in described regenerator degassing vessel (8) cavity is provided with the degassed dielectric distribution ring (25) of regenerator for being uniformly distributed the degassed medium of regenerator sending into described regenerator degassing vessel (8).
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| CN107540498A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether conversion preparing aromatic hydrocarbon and low-carbon alkene |
| CN107540492A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540496A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540495A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107540498A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether conversion preparing aromatic hydrocarbon and low-carbon alkene |
| CN107540492A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540496A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540495A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene |
| CN108017484A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of high arenes selectivity during maintenance methanol aromatic hydrocarbons |
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