CN103450921A - Method for selectively preparing propylene and clean gasoline through using methanol - Google Patents
Method for selectively preparing propylene and clean gasoline through using methanol Download PDFInfo
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- CN103450921A CN103450921A CN2012101797638A CN201210179763A CN103450921A CN 103450921 A CN103450921 A CN 103450921A CN 2012101797638 A CN2012101797638 A CN 2012101797638A CN 201210179763 A CN201210179763 A CN 201210179763A CN 103450921 A CN103450921 A CN 103450921A
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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Abstract
The invention relates to a method for selectively preparing propylene and clean gasoline through using methanol. The method comprises the following steps: methanol enters a double arc bottom turbulent bed reactor through a methanol feeding ring tube to contact and react with a catalyst at 300-500DEG C for 2-5s; an obtained gas enters a conveying bed reactor after reducing, wherein the gas retention time is 1-3s; the gas and the catalyst are separated by a cyclone separator in a settlement device, and the gas gets away off a reaction regeneration system separating system from the top of the settlement device to a separation system; the settled catalyst is added to a reactivator for scorching regeneration; and the regenerated catalyst returns to the double arc bottom turbulent bed reactor, and a pre-riser outlet is arranged on a cross section in which a highest nozzle outlet of the feeding ring tube. The methanol conversion rate is 99.48wt%, generated hydrocarbons contain higher-content gasoline, lower-content liquefied gas and lowest-content dry gas and coke, the content of propylene in the liquefied gas reaches 62.13%, and the content of ethylene in the dry gas reaches 82wt%.
Description
Technical field:
The present invention relates to a kind of method for methyl alcohol selectively producing propene and clean gasoline.
Background technology
Mobil Corp. (Mobil) has proposed a kind of use ZSM-5 catalyzer, carries out the technical process of preparing olefin by conversion of methanol in shell and tube reactor, and carries out the pilot experiment of 9 months in 1984, and experimental scale is 100 barrels/day.In technological process, methyl alcohol is diffused in catalyst pores and is reacted, and at first generates dme, then generates ethene, reaction is proceeded, generate propylene, butylene and higher alkene, also can generate dipolymer and ring compound, take carbon selectivity as basis, it is heavy that yield of ethene can reach 60%(), it is heavy that the alkene total recovery can reach 80%(), the twice in adopting conventional petroleum naphtha/gas oil pyrolysis in tubular furnace method yield about the same, but the life-span of catalyzer is still undesirable.
BASF AG (BASF) adopts zeolite catalyst, has set up the pilot plant of 30 tons of methyl alcohol of a set of daily consumption in summer in 1980 at Ludwigshafen, Germany.Its temperature of reaction is 300-450 ℃, and pressure is 0.1-0.5Mpa, with various zeolites, makees catalyzer, and Preliminary experiment results is that the weight yield of C2-C4 alkene is 50-60%, and yield is too low.
The catalyzer that Praxair Technology, Inc (UOP) filters out is called MTO-100.MTO-100 is the combination of the tamanori material of the SAPO-34 of union carbide corporation exploitation and a series of special selections.SAPO-34 is the matrix of MTO-100 catalyzer, and the eighties in 20th century, by the exploitation of Union Carbide molecule sieve part, main chemical compositions comprises the elements such as silicon (Si), aluminium (Al), phosphorus (P), oxygen (O).It has suitable inner duct scantlings of the structure and solid acid intensity, can reduce the alkene generation oligomerisation reaction generation macromolecule hydrocarbon that initial reaction stage generates as far as possible, thereby improve target product--the selectivity of alkene.Although SPAO-34 is desirable catalytic material, be not robust material to fluidized bed process, and selected tamanori can increase catalyst strength and wear resistance.By inference, the tamanori adopted in MTO-100 is silicon-dioxide and the aluminum oxide of processing.SAPO-34 molecular sieve catalyst aperture only allows ethene, propylene and a small amount of C
4by, can not produce heavy hydrocarbon products.Ethene, propylene ratio can be regulated between 0.75～1.5, the productive rate of ethene+propylene more stable (80% left and right), and also the purity of ethene and propylene can directly meet the requirement of polymerization-grade propylene and ethene all more than 99.6%.
Ac.cn, as the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences, University of Petroleum, Shi Ke institute of China Petrochemical Industry have also carried out the research of similar catalyzer, obtained the result approaching with UOP, and this has turned preparation into for from now on domestic of catalyzer.
The MTO process using is similar to ripe FCC processing method, it is the fluid catalytic cracking technology that conversion reaction and catalyzer coke burning regeneration carry out continuously, constantly the catalyzer after compensation regeneration, guarantee that the reactive behavior of catalyzer and selectivity are stable, and conversion reaction is steadily carried out.
UOP and Hai De company (Norsk Hydro) have built in cooperation in June nineteen ninety-five the MTO technique demonstration unit that a set of thick methyl alcohol working ability is 0.75t/d, have installed continuous operation 90 days, and the operation of each system is normal, stable.In running in 90 days, catalyzer is through 450 secondary responses-reprocessing cycle, and its performance is still highly stable, and after reaction, by sampling analysis, the intensity of catalyzer also meets the demands, and can change the yield ratio that operational condition is regulated ethene and propylene.The purity of ethene and propylene, all more than 99.6%, can directly meet the requirement of polymerization-grade propylene and ethene.
Praxair Technology, Inc in November nineteen ninety-five (UOP) and Hai Deluo company (Norsk Hydro) have announced first their the natural gas via synthesizing methanol of joint development and have further produced the MTO process of alkene (ethene, propylene and butylene) and the service data of demonstration unit in the 4th the conversion of natural gas international conference in South Africa, and claim this process can realize producing per year the suitability for industrialized production of 500,000 tons of ethene, can obtain the license licensed licenser licence of founding the factory from Praxair Technology, Inc (UOP), Hai Deluo company (Norsk Hydro).
The gas chemical industry associated enterprises that is positioned at Nigeria adopts the MTO technique of UOP/Hydro company exploitation, material benzenemethanol comes from the 7500t/d methanol device, 400,000 ton/years of ethene and 400,000 ton/years of propylene are produced in the MTO design, ethene and propylene are used further to produce 400,000 ton/years of HDPE and 400,000 ton/years of PP, in 2003, completed basic design, this machinery was gone into operation due to 2006.Norway and the Middle East are also utilizing this technology to carry out design and the planning in early stage of 200,000 tons and 500,000 tons ethene.
From a large amount of bibliographical informations, the catalyzer aspect, the purpose product is if ethene, and active ingredient is all the SAPO-34 molecular sieve basically; If the purpose product is propylene or gasoline, active ingredient is generally ZSM-5 molecular sieve.The reactor aspect, considerably less (patent: US4929780 with fixed bed, CN 1084431A), majority is all to adopt fluidized-bed, but, the form of the fluidized-bed that different technology adopts varies, some employings be fast bed (US6166282, US4076796), a bed (CN 1688522A is carried in some employings, CN2339296Y, US 7385099B2), some employing turbulent beds (CN 101152998A, CN 101172937A, CN101172936A), the employing fast bed+turbulent bed (US 4328384) had.
Summary of the invention
The purpose of this invention is to provide a kind of method for methyl alcohol selectively producing propene and clean gasoline.With the difference of disclosed patent, be: 1. the active ingredient of catalyzer is nanometer rod grafting ZSM-11 Quito level porous molecular sieve material (synthetic method has been applied for national inventing patent CN201210003750.5); 2. reactor adopts instantaneous contact high-density turbulent bed+conveying bed; 3. the purpose product is clean gasoline with high octane and propylene, and both ratios can be adjusted flexibly by the silica alumina ratio of adjusting ZSM-11.
Method for methyl alcohol selectively producing propene and clean gasoline of the present invention; Comprise that methanol oxidation transforms the catalyzer of stop bracket gasoline processed and propylene and the circulating fluidized bed reaction regeneration device be complementary with this catalyzer.
The method synthetic nanometer rod grafting ZSM-11 Quito level porous molecular sieve material of the active ingredient of catalyzer for announcing by CN201210003750.5, this material has abundant micropore and mesopore, and micropore canals is straight and short, be convenient to methyl alcohol to the diffusion in hole and product to the hole external diffusion, reduce propylene and change into alkane.The content of this molecular screen material in the catalyzer prepared through mist projection granulating accounts for 5～50wt%.Other component of catalyzer (catalyzer prepared by the mist projection granulating of all take is benchmark) also comprises kaolin (5～50wt%), silicon-dioxide (0.1～20wt%, from the silicon sol as binding agent, be transformed), aluminium sesquioxide (0.1～20wt%, from the aluminium colloidal sol as binding agent or the pseudo-boehmite of acidifying, be transformed), Vanadium Pentoxide in FLAKES (0.1～15wt%, before mist projection granulating, the phosphoric acid in slurries is transformed again).
Methyl alcohol reacts on the catalyzer of preparation as stated above, make methyl alcohol fully transform, except temperature of reaction must, at 300 ° of C with upper outside, also must guarantee that methyl alcohol can fully contact with catalyzer; Want selectivity to produce gasoline and propylene, except temperature of reaction can not surpass 500 ° of C, also must strictly control gas (product generated after nail alcohol and reaction thereof) and can not surpass 10s solid (referring to catalyzer) duration of contact, be preferably in 5s; In the methyl alcohol reaction process, catalyzer can coking deactivation, but deactivation rate is unhappy, and at fixing bed reaction, catalyzer because of time of carbon deposit inactivation difference difference because of concrete reaction conditions, generally arrives dozens of minutes at several minutes fully; Here the catalyzer of use belongs to solid acid catalyst, if the alkene that the methyl alcohol reaction generates can not separate in time with catalyzer, alkene hydrogen transfer reactions can occur and changes into alkane, thereby reactor should reduce the back-mixing of gas as far as possible; In addition, in the gasoline that methyl alcohol reaction generates, if transform insufficiently, may contain a certain amount of oxygenatedchemicals, thereby must allow these oxygenatedchemicalss fully transform, to guarantee quality of gasoline.For above-mentioned requirements, invented and take as shown in drawings " instantaneous contact turbulent bed+conveying bed " but be the successive reaction of reactor and the circulating fluidized bed device of regeneration.
In the turbulent bed of dense fluidized, be to guarantee methyl alcohol and catalyzer high-efficient contact and the abundant key transformed.For this reason, methyl alcohol adopts the endless tube charging, and the feed nozzle on endless tube is totally downward direction, and each nozzle can be different from the angle of reactor axis direction; For guaranteeing catalyst distribution as far as possible evenly, the profile from reactor along axis, bottom is two circular arc bottom structures; For guaranteeing steadily fluidisation of catalyzer, the pre-lift pipe export at least will the jet exit residing cross section the highest in charging endless tube position on.Blank pipe gas by the gas generated after methanol conversion under the real reaction condition is calculated quickly, and the mean residence time of gas in turbulent bed can not surpass 5s, is preferably in 2s.Turbulent bed top, through undergauge, is connected with transport bed reactor, and oil gas starts undergauge from turbulent bed and exports to transport bed reactor, and the mean residence time of gas (calculating by the real reaction condition) is not more than 5s, preferably is less than 3s.With what carry the bed top to be connected, be settling vessel, in settling vessel, gas with catalyzer after cyclonic separator separates, gas leaves reaction-regeneration system from the settling vessel top, get separation system, the catalyzer settled down enters revivifier through inclined tube to be generated, carries out the coke burning regeneration of catalyzer with air; If the coke on catalyzer burning is not enough to maintain the needed temperature condition of catalyst regeneration, can add warm air at the auxiliary chamber afterburning, also direct afterburning in revivifier.Catalyzer after regeneration enters reactor bottom through regenerator sloped tube, and the dry gas generated through water vapor or reaction carries out pre-lift, and catalyzer is returned in the turbulent bed reactor.
Major technique advantage of the present invention is the following aspects:
(1) to take the nanometer rod grafting ZSM-11 multi-stage porous molecular screen material that hangs down diffusional resistance be active ingredient to catalyzer, has a high added value product yield high, and gasoline octane rating is high, the advantages such as Propylene Selectivity height.
(2) reactor combines the turbulent bed reactor of instantaneous contact dense fluidized with the transport bed reactor of low fluid density, the turbulent bed reactor is also by the innovation of structure and feeding manner, reduce the channeling that turbulent bed occurs usually, thereby improve gas-solid contact efficiency.The turbulent bed reactor of high gas-solid contact efficiency guarantees that methyl alcohol fully contacts and reacts with catalyzer, thereby guarantees the transformation efficiency of methyl alcohol; In the turbulent bed of dense fluidized, the residence time of gas is short, can reduce back-mixing and the secondary reaction of propylene.The transport bed reactor fluid density is low, if can reduce the secondary reaction of the propylene of adsorptive power, guarantees the selectivity of propylene; Carry the fluid density that bed is low, do not hinder absorption and the reaction of the oxygenatedchemicals in the gasoline fraction of high adsorption capacity, thereby guarantee the abundant conversion of oxygenatedchemicals in gasoline fraction.
(3) ratio of gasoline and propylene, can be adjusted than neatly by the Si/Al that adjusts the ZSM-11 molecular screen material, also can adjust by adjusting temperature of reaction.
The accompanying drawing explanation
Fig. 1 reaction and reprocessing cycle fluidizer
Wherein: 1. methanol feeding endless tube; 2. pre-lift pipe; 3. turbulent bed reactor at the bottom of two arcs; 4. pre-lift medium; 5. regenerator sloped tube; 6. air; 7. revivifier; 8. flue gas; 9. inclined tube to be generated; 10. settling vessel; 11. the gas that reaction generates; 12. transport bed reactor.
Embodiment
Method for methyl alcohol selectively producing propene and clean gasoline of the present invention comprises that methanol oxidation transforms the catalyzer of stop bracket gasoline processed and propylene and the circulating fluidized bed reaction regeneration device be complementary with this catalyzer; Methanol feedstock enters turbulent bed reactor 3 at the bottom of two arcs by the methanol feeding endless tube 1 that is positioned at pre-lift pipe 2 outlet top, downward by general direction on endless tube, at the bottom of the feed nozzle different from the angle of reactor axis direction sprays to two arcs, the turbulent bed reactor bottom reacts with the catalyzer uniform contact; Temperature of reaction is at 300～500 ° of C, and the time is 2～5s; At the bottom of two arcs, turbulent bed reactor 3 tops through undergauges, are connected with transport bed reactor 12, and oil gas exports to transport bed reactor from turbulent bed reactor 3 beginning undergauges at the bottom of two arcs, and the mean residence time of gas is 1～3s; What with the transport bed reactor top, be connected is settling vessel 10, and in settling vessel, gas is with catalyzer after cyclonic separator separates, and the gas that reaction generates leaves reaction-regeneration system and goes separation system from the settling vessel top; The catalyzer settled down enters revivifier 7 through inclined tube 9 to be generated, carries out the coke burning regeneration of catalyzer with air 6; Catalyzer after regeneration enters pre-lift pipe 2 bottoms through regenerator sloped tube 5, carry out pre-lift through pre-lift medium 4, catalyzer is returned at the bottom of two arcs in the turbulent bed reactor, and 2 outlets of pre-lift pipe are located on the highest residing cross section of jet exit in charging endless tube position.
Embodiment 1:
The pseudo-boehmite that adds 11.76kg in stirring tank, inject the 700kg deionized water, and adding the salt acid for adjusting pH value under the condition of continuously stirring is 3-4.After pseudo-boehmite changes into jelly fully, add in still that 60kg's change into the ZSM-11 molecular screen material (SiO of Hydrogen through ion-exchange
2/ Al
2o
3than being 100), then add 106kg kaolin, after stirring, then add 40kg silicon sol and 14kg phosphoric acid.After stirring 2h, carry out mist projection granulating.
The microspherical catalyst obtained is standby after aging 4h under 800 ° of C, 100% water vapor condition.
In the pilot plant that catalyzer 50kg after aging is packed into by structure building shown in the drawings.Temperature of reaction in turbulent bed is controlled at 420 ° of C; The average linear velocity of gas in turbulent bed is 0.45m/s, and mean residence time is about 2s; The average linear speed of gas in carrying bed is 7m/s, and mean residence time is about 1.5s.Temperature in revivifier is controlled at 700 ° of C, and the amount of air is to guarantee that carbon deposit on catalyzer dryouies (coke content ≯ 0.15wt% on regenerator) only fully and is advisable.
Take pure methyl alcohol as raw material, and inlet amount is 40kg/h, and reaction result is as shown in subordinate list.
Measure the methanol content in water, the methanol conversion calculated thus is 99.48wt%, almost completely transforms.In reaction product, the yield of water is close to theoretical value 56wt%; In the hydrocarbon generated, the amount of gasoline is maximum, is secondly liquefied gas, and the yield of dry gas and coke is all very low.In liquefied gas, the content of propylene has reached 62.13%; More than in dry gas, the content of ethene has reached 82wt% especially.
Reaction result in subordinate list, absolutely proved that the catalyzer invented and supporting reactor transform selectivity at methanol oxidation and produce the excellent properties aspect gasoline and propylene.
1. subordinate list
The methyl alcohol distribution of reaction products
Claims (2)
1. the method for methyl alcohol selectively producing propene and clean gasoline is characterized in that:
The catalyzer that the nanometer rod grafting ZSM-11 multilevel hole material of take is active ingredient, be equipped with circulating fluidized bed reaction regeneration device, for the methyl alcohol selective catalysis transform to produce take clean stop bracket gasoline as main oil product, take propylene as main low-carbon alkene product;
Methanol feedstock enters turbulent bed reactor at the bottom of two arcs by the methanol feeding endless tube that is positioned at pre-lift pipe outlet top, downward by general direction on endless tube, at the bottom of the feed nozzle different from the angle of reactor axis direction sprays to two arcs, the turbulent bed reactor bottom reacts with the catalyzer uniform contact; Temperature of reaction is at 300～500 ° of C, and the time is 2～5s; At the bottom of two arcs, turbulent bed reactor top through undergauge, is connected with transport bed reactor, and oil gas starts undergauge from turbulent bed reactor at the bottom of two arcs and exports to transport bed reactor, and the mean residence time of gas is 1～3s; What with the transport bed reactor top, be connected is settling vessel, and in settling vessel, gas is with catalyzer after cyclonic separator separates, and the gas that reaction generates leaves reaction-regeneration system and goes separation system from the settling vessel top; The catalyzer settled down enters revivifier through inclined tube to be generated, carries out the coke burning regeneration of catalyzer with air; Catalyzer after regeneration enters pre-lift pipe bottom through regenerator sloped tube, through the pre-lift medium, carries out pre-lift, and catalyzer is returned at the bottom of two arcs in the turbulent bed reactor, and the outlet of pre-lift pipe is located on the highest residing cross section of jet exit in charging endless tube position.
2. the method for methyl alcohol selectively producing propene and clean gasoline according to claim 1 is characterized in that: the profile of turbulent bed reactor from reactor along axis at the bottom of two arcs, bottom is two circular arc bottom structures.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018129B (en) * | 2014-04-18 | 2017-01-18 | 中石化洛阳工程有限公司 | Device and method for producing gasoline from methyl alcohol by fluidized bed |
| CN108654526A (en) * | 2017-04-01 | 2018-10-16 | 中国石油大学(华东) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing |
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| US4049573A (en) * | 1976-02-05 | 1977-09-20 | Mobil Oil Corporation | Zeolite catalyst containing oxide of boron or magnesium |
| CN1356927A (en) * | 1999-05-20 | 2002-07-03 | 埃克森美孚化学专利公司 | Metal-contg. macrostructures of porous inorganic oxide, prepn. thereof, and use |
| CN1678715A (en) * | 2002-08-01 | 2005-10-05 | 埃克森美孚化学专利公司 | Two stage hydrocarbon conversion reaction system |
| JP2007290991A (en) * | 2006-04-24 | 2007-11-08 | Idemitsu Kosan Co Ltd | Method for producing olefin from oxygen-containing compound |
| CN101244971A (en) * | 2008-02-27 | 2008-08-20 | 大连理工大学 | Synthesis method for producing ethylene with high-efficiency dehydration of biological ethyl alcohol |
| US20100099925A1 (en) * | 2008-10-16 | 2010-04-22 | Range Fuels, Inc. | Methods and apparatus for synthesis of alcohols from syngas |
-
2012
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4049573A (en) * | 1976-02-05 | 1977-09-20 | Mobil Oil Corporation | Zeolite catalyst containing oxide of boron or magnesium |
| CN1356927A (en) * | 1999-05-20 | 2002-07-03 | 埃克森美孚化学专利公司 | Metal-contg. macrostructures of porous inorganic oxide, prepn. thereof, and use |
| CN1678715A (en) * | 2002-08-01 | 2005-10-05 | 埃克森美孚化学专利公司 | Two stage hydrocarbon conversion reaction system |
| JP2007290991A (en) * | 2006-04-24 | 2007-11-08 | Idemitsu Kosan Co Ltd | Method for producing olefin from oxygen-containing compound |
| CN101244971A (en) * | 2008-02-27 | 2008-08-20 | 大连理工大学 | Synthesis method for producing ethylene with high-efficiency dehydration of biological ethyl alcohol |
| US20100099925A1 (en) * | 2008-10-16 | 2010-04-22 | Range Fuels, Inc. | Methods and apparatus for synthesis of alcohols from syngas |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018129B (en) * | 2014-04-18 | 2017-01-18 | 中石化洛阳工程有限公司 | Device and method for producing gasoline from methyl alcohol by fluidized bed |
| CN108654526A (en) * | 2017-04-01 | 2018-10-16 | 中国石油大学(华东) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing |
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