CN102875304B - Method for preparing low carbon olefins from methanol and naphtha - Google Patents
Method for preparing low carbon olefins from methanol and naphtha Download PDFInfo
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- CN102875304B CN102875304B CN201110195291.0A CN201110195291A CN102875304B CN 102875304 B CN102875304 B CN 102875304B CN 201110195291 A CN201110195291 A CN 201110195291A CN 102875304 B CN102875304 B CN 102875304B
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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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- 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
- Y02P30/40—Ethylene production
Abstract
The invention relates to a method for preparing low carbon olefins from methanol and naphtha to mainly solve a low yield problem of the low carbon olefins in the prior art. The method comprises the following steps: allowing a naphtha raw material to enter a riser I and a methanol raw material to enter a riser II in order to respectively contact with a catalyst, mixing the low carbon olefins contained products generated in the riser I and the riser II, allowing the obtained mixture to enter a separation segment, and separating to obtain low carbon olefin products, wherein the riser I is connected with the riser II in an axial direction through an exchange zone, the inside of the riser I, the inside of the riser II and the inside of the exchange zone are communicated, the axial height of the connection side surface of the exchange zone and the riser I or the riser II in the axial direction is 1/3-4/5 of the height of the riser I, and the radial height of the connection side surface is 1/5-3/4 of the diameter of the riser I. The above technical scheme well solves the problem, so the method can be used for the industrial production of the low carbon olefins.
Description
Technical field
The present invention relates to a kind of method that low-carbon alkene prepared by methyl alcohol and petroleum naphtha.
Technical background
Low-carbon alkene, i.e. ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are produced by petroleum path, but due to the limited supply of petroleum resources and higher price, produce ethene by petroleum resources, the cost of propylene constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials for light olefin production of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, and as methyl alcohol, can be obtained by coal or Sweet natural gas, technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to the popularity in oxygenatedchemicals source, add the economy transforming and generate light olefin technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), be particularly subject to increasing attention by the technique of preparing olefin by conversion of methanol (MTO).
Petroleum naphtha is a kind of light-end products, is cut corresponding cut by crude distillation or oil secondary processing and is obtained.Its boiling spread is determined according to need, is generally wider boiling range, as 20-220 DEG C.Petroleum naphtha is pyrolysis in tubular furnace preparing ethylene, and propylene and catalytic reforming produce the important source material of benzene,toluene,xylene.As cracking stock, in requiring petroleum naphtha to form, the content of alkane and naphthenic hydrocarbon is not less than 70% (volume).Naphtha catalytic pyrolysis preparing low-carbon alkene is then under catalyzer existent condition, carries out cracking to obtain the production process of low-carbon alkene to petroleum hydrocarbon.Compare with traditional tube furnace steam heat cracking, this process reaction temperature is about lower than steam cracking reaction 50 ~ 200 DEG C, and energy consumption significantly reduces; Cracking furnace pipe inwall coking rate also can reduce, thus can prolong operation cycle, increases the boiler tube life-span; Carbon emission simultaneously also can reduce, and alleviates pollution, and can adjust the product mix flexibly.
Technology and reactor that a kind of oxygenate conversion is low-carbon alkene is disclosed in US6166282, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, after rising to the fast subregion that internal diameter diminishes rapidly, special gas-solid separation equipment initial gross separation is adopted to go out most entrained catalyst.Due to reaction after product gas and catalyzer sharp separation, effectively prevent the generation of secondary reaction.Through analog calculation, compared with traditional bubbling fluidization bed bioreactor, needed for this fast fluidized bed reactor internal diameter and catalyzer, reserve all greatly reduces.
The multiple riser reaction unit disclosed in CN1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactor, gas solid separation district, multiple offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and gas product are separated.But there is the lower shortcoming of yield of light olefins in the method.
Disclose a kind of method of methanol production propylene in EP0448000 and EP0882692, first methyl alcohol be converted into DME and water, then mixture is transported to First reactor, and add steam in this reactor.In the first reactor, methyl alcohol and (or) dme or its mixture and catalyst exposure react, catalyzer adopts the special ZSM-5 catalyzer containing ZnO and CdO, temperature of reaction 280 ~ 570 DEG C, pressure 0.01 ~ 0.1MPa, preparing with propylene is the product of main hydro carbons.Heavier product is as C
5 +hydrocarbon continues to carry out reacting the hydro carbons be converted into based on propylene in second reactor, after cooling, send separator back to.Product is compressed, refining further after can obtain the chemical grade propylene that purity is 97%.But adopt multiple fixed-bed reactor in this technique, because the activity of catalyzer limits, therefore need frequent blocked operation, and heat-obtaining problem is also very complicated.
US 20070083071 discloses the processing method that a kind of hydrocarbon catalytic pyrolysis produces ethene, propylene, hydrocarbon feed is converted into the product comprising low-carbon alkene in catalytic cracker, then product stream is separated into C2 ~ C3 alkane, C2 ~ C3 alkene, the three kinds of logistics of C4+ hydrocarbon by series of process, C2 ~ C3 alkane is returned tube cracking furnace and carries out thermo-cracking, C4+ hydrocarbon returns catalytic cracker and carries out catalytic pyrolysis, finally obtains the ethene of higher yields, propylene product.The method adopts riser reactor, and reactant residence time is shorter, and low-carbon alkene product once through yield is lower.
Due to naphtha catalytic cracking and preparing olefin by conversion of methanol react object product---low-carbon alkene is identical, and main ingredient kind separately in product is roughly the same, the catalyst system adopted is also roughly the same, and from reaction mechanism angle, all there is the process being cracked into small molecules hydro carbons by macromole hydrocarbon or intermediate, therefore these two kinds of Technologies are had ready conditions and are coupled.Prior art still not in same reactor by precedent that two kinds of technology are coupled.The present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that the yield of light olefins that exists in prior art is not high, provides a kind of new methyl alcohol and petroleum naphtha to prepare the method for low-carbon alkene.The method is used for, in the production of low-carbon alkene, having the advantage that yield of light olefins is higher.
For solving the problem, the technical solution used in the present invention is as follows: the method for low-carbon alkene prepared by a kind of methyl alcohol and petroleum naphtha, the raw material comprising petroleum naphtha enters riser tube I, comprise the raw material of methyl alcohol enters riser tube II, respectively with catalyst exposure, after the product stream comprising low-carbon alkene generated in riser tube I and riser tube II mixes, enter centrifugal station, be isolated to low-carbon alkene product; Wherein, described riser tube I is connected by switched area with on riser tube II axial direction due, and the inside of riser tube I, riser tube II, switched area is in connected state, switched area axial direction due is 1/3 ~ 4/5 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 1/5 ~ 3/4 of riser tube I diameter.
In technique scheme, described catalyzer comprises ZSM-5 molecular sieve, SiO
2/ Al
2o
3mol ratio is 10 ~ 100; Described catalyzer is the catalyzer after regeneration, and catalyzer coke content massfraction is 0.01 ~ 0.5%; Also comprise water vapour in described riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 0.05 ~ 1.5: 1; Also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 30 ~ 70%; Described petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C; In described riser tube I, reaction conditions is: temperature of reaction is 570 ~ 670 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 530 ~ 630 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; The product stream comprising low-carbon alkene generated in described riser tube I and riser tube II enters same settling vessel, in settling vessel, isolated reclaimable catalyst goes revivifier to regenerate through inclined tube to be generated, and the regenerated catalyst after regeneration returns to the buffer zone bottom riser tube I and riser tube II; Carbon four ~ carbon eight hydrocarbon that described centrifugal station is separated can inject in corresponding riser tube along at least one opening for feed that riser tube I or riser tube II axial direction due separate.
In the present invention, slightly revolve and refer to and be positioned at riser tube or down-flow fluidized bed using ECT outlet can realize the primary cyclone of gas-solid sharp separation, due to its separation efficiency lower (generally between 70 ~ 90%), therefore those skilled in the art is generally simply referred to as " slightly revolving ".
Adopt method of the present invention, two riser tubes are set, and two riser tube inside are in connected state, connected by switched area, it is low-carbon alkene that a riser tube is mainly used in naphtha catalytic cracking, a riser tube is mainly used in carbon four ~ carbon five hydrocarbon by product of catalyzed conversion methyl alcohol and generation, with as far as possible many production low-carbon alkenes.By arranging switched area between two riser tubes, be conducive to the phase mutual diffusion between methyl alcohol or feed naphtha and product.The present inventor is found by research, adds the generation that methyl alcohol can promote naphtha cracking in naphtha catalytic cracking reaction process.The existence of switched area, not only make the gas-solid phase phase mutual diffusion of two riser tube inside, mutually promote, but also mutually play the object reducing feed partial pressure, simultaneously because naphtha catalytic cracking is thermo-negative reaction, and methanol oxidation is converted into low-carbon alkene is strong exothermal reaction, so the exchange of gas-solid material also helps the mutual balance of heat in two riser tubes.Achieve good effect.Therefore, adopt method of the present invention, not only can reach the object improving yield of light olefins, and be conducive to the optimization of energy.
Adopt technical scheme of the present invention: described catalyzer comprises ZSM-5 molecular sieve, SiO
2/ Al
2o
3mol ratio is 10 ~ 100; Described catalyzer is the catalyzer after regeneration, and catalyzer coke content massfraction is 0.01 ~ 0.5%; Also comprise water vapour in described riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 0.05 ~ 1.5: 1; Also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 30 ~ 70%; Described petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C; In described riser tube I, reaction conditions is: temperature of reaction is 570 ~ 670 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 530 ~ 630 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; The product stream comprising low-carbon alkene generated in described riser tube I and riser tube II enters same settling vessel, in settling vessel, isolated reclaimable catalyst goes revivifier to regenerate through inclined tube to be generated, and the regenerated catalyst after regeneration returns to the buffer zone bottom riser tube I and riser tube II; Carbon four ~ carbon eight hydrocarbon that described centrifugal station is separated can inject in corresponding riser tube along at least one opening for feed that riser tube I or riser tube II axial direction due separate, and low-carbon alkene carbon base absorption rate can reach 59.41% weight, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
Fig. 2 is the A-B sectional view in Fig. 1.
In Fig. 1,1 for promoting steam-in pipeline; 2 is buffer zone; 3 is riser tube II feeding line; 4 is riser tube I feeding line; 5 is switched area; 6 is regenerator sloped tube; 7 is riser tube I; 8 is riser tube II; 9 is riser tube I side feed opening; 10 is riser tube II side feed opening; 11 is stripping stage; 12 slightly revolve for leg outlet; 13 slightly revolve for leg outlet; 14 is stripping fluid source line; 15 is settling vessel; 16 is gas-solid cyclone separator; 17 is products export pipeline; 18 is inclined tube to be generated.
The raw material comprising petroleum naphtha enters riser tube I 7, comprise the raw material of methyl alcohol enters riser tube II 8, respectively with catalyst exposure, after the product stream comprising low-carbon alkene generated in riser tube I 7 and riser tube II 8 mixes in settling vessel 15, enter centrifugal station, be isolated to low-carbon alkene product.In settling vessel 15, isolated reclaimable catalyst enters revivifier regeneration through inclined tube 18 to be generated after stripping stage 11 stripping, and the regenerated catalyst after regeneration enters buffer zone 2 through regenerator sloped tube 6.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In reaction unit as shown in Figure 1, catalyzer is ZSM-5, and the massfraction that ZSM-5 molecular sieve accounts for catalyzer is 42%, SiO
2/ Al
2o
3mol ratio is 100, and all the other are binding agent SiO
2the raw material comprising petroleum naphtha enters riser tube I, comprise the raw material of methyl alcohol enters riser tube II, respectively with catalyst exposure, after the product stream comprising low-carbon alkene generated in riser tube I and riser tube II mixes in settling vessel, enter centrifugal station, be isolated to low-carbon alkene product; Wherein, riser tube I is connected by switched area with on riser tube II axial direction due, and the inside of riser tube I, riser tube II, switched area is in connected state, switched area axial direction due is 4/5 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 3/4 of riser tube I diameter.In settling vessel, isolated reclaimable catalyst goes revivifier to regenerate through inclined tube to be generated, and the regenerated catalyst after regeneration returns to the buffer zone bottom riser tube I and riser tube II.Regenerated catalyst coke content massfraction is 0.5%, also water vapour is comprised in riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 1.5: 1, also comprises carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated, wherein olefin content 70% in riser tube II charging.Petroleum naphtha boiling range is in table 1.In riser tube I, reaction conditions is: temperature of reaction is 670 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 630 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds.Riser tube I and riser tube II is along respective axial direction due being arranged two opening for feeds, riser tube I side feed opening position is respectively apart from bottom riser tube I being 1/3,1/2 riser tube I height, riser tube II side feed opening position is respectively apart from being 1/3,1/2 riser tube II height bottom riser tube I, and carbon four ~ carbon eight hydrocarbon that centrifugal station is separated injects in corresponding riser tube along the opening for feed on riser tube I or riser tube II axial direction due.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 57.09% weight.
Table 1 petroleum naphtha typical case composition
| Initial boiling point, DEG C | 40 |
| Final boiling point, DEG C | 162 |
| Positive structure and isoparaffin, % by weight | 65.18 |
| Alkene, % by weight | 0.17 |
| Naphthenic hydrocarbon, % by weight | 28.44 |
| Aromatic hydrocarbons, % by weight | 6.21 |
[embodiment 2]
According to the condition described in embodiment 1 and step, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 10, switched area axial direction due is 1/3 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 1/5 of riser tube I diameter.Regenerated catalyst coke content massfraction is 0.01%, also water vapour is comprised in riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 0.05, and also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 31%.Petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C.In riser tube I, reaction conditions is: temperature of reaction is 570 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 530 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds.Riser tube I and riser tube II is along respective axial direction due being arranged an opening for feed, it is 1/2 riser tube I height bottom riser tube I side feed opening positional distance riser tube I, be 1/2 riser tube II height bottom riser tube II side feed opening positional distance riser tube I, carbon four ~ carbon eight hydrocarbon that centrifugal station is separated injects in corresponding riser tube along the opening for feed on riser tube I or riser tube II axial direction due.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 55.27% weight.
[embodiment 3]
According to the condition described in embodiment 1 and step, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 70, switched area axial direction due is 1/2 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 2/5 of riser tube I diameter.Regenerated catalyst coke content massfraction is 0.1%, also water vapour is comprised in riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 0.5, and also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 46%.Petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C.In riser tube I, reaction conditions is: temperature of reaction is 635 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 600 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 59.41% weight.
[embodiment 4]
According to the condition described in embodiment 1 and step, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 160, switched area axial direction due is 1/2 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 1/5 of riser tube I diameter.Regenerated catalyst coke content massfraction is 0.18%, also water vapour is comprised in riser tube I charging, the weight ratio of water vapour and petroleum naphtha is 0.5, and also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 46%.Petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C.In riser tube I, reaction conditions is: temperature of reaction is 650 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 610 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 54.11% weight.
[comparative example 1]
According to the condition described in embodiment 1 and step, just do not arrange switched area, low-carbon alkene carbon base absorption rate is 50.88% weight.
Obviously, adopt method of the present invention, the object improving yield of light olefins can be reached, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (6)
1. the method for low-carbon alkene prepared by a methyl alcohol and petroleum naphtha, the raw material comprising petroleum naphtha enters riser tube I, comprise the raw material of methyl alcohol enters riser tube II, respectively with catalyst exposure, after the product stream comprising low-carbon alkene generated in riser tube I and riser tube II mixes, enter centrifugal station, be isolated to low-carbon alkene product; Wherein, described riser tube I is connected by switched area with on riser tube II axial direction due, and the inside of riser tube I, riser tube II, switched area is in connected state, switched area axial direction due is 1/3 ~ 4/5 of riser tube I height with the axial height of the connection side on riser tube I or riser tube II axial direction due, radial width is 1/5 ~ 3/4 of riser tube I diameter; Described catalyzer is the catalyzer after regeneration, and catalyzer coke content massfraction is 0.01 ~ 0.5%; Carbon four ~ carbon eight hydrocarbon that described centrifugal station is separated can inject in corresponding riser tube along at least one opening for feed that riser tube I or riser tube II axial direction due separate.
2. the method for low-carbon alkene prepared by methyl alcohol and petroleum naphtha according to claim 1, it is characterized in that described catalyzer comprises ZSM-5 molecular sieve, SiO
2/ Al
2o
3mol ratio is 10 ~ 100.
3. the method for low-carbon alkene prepared by methyl alcohol and petroleum naphtha according to claim 1, it is characterized in that also comprising water vapour in described riser tube I charging, and the weight ratio of water vapour and petroleum naphtha is 0.05 ~ 1.5: 1; Also comprise carbon four ~ carbon five hydrocarbon mixture that described centrifugal station is separated in riser tube II charging, wherein olefin content is 30 ~ 70%.
4. the method for low-carbon alkene prepared by methyl alcohol and petroleum naphtha according to claim 1, it is characterized in that described petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C.
5. the method for low-carbon alkene prepared by methyl alcohol and petroleum naphtha according to claim 1, it is characterized in that in described riser tube I, reaction conditions is: temperature of reaction is 570 ~ 670 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; In riser tube II, reaction conditions is: temperature of reaction is 530 ~ 630 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds.
6. the method for low-carbon alkene prepared by methyl alcohol and petroleum naphtha according to claim 1, it is characterized in that the product stream comprising low-carbon alkene generated in described riser tube I and riser tube II enters same settling vessel, in settling vessel, isolated reclaimable catalyst goes revivifier to regenerate through inclined tube to be generated, and the regenerated catalyst after regeneration returns to the buffer zone bottom riser tube I and riser tube II.
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| WO2016018097A1 (en) * | 2014-08-01 | 2016-02-04 | 한국화학연구원 | Naphtha and methanol mixed catalytic cracking reaction process |
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| CN101992046A (en) * | 2009-08-31 | 2011-03-30 | 中国石油化工股份有限公司上海石油化工研究院 | Parallel combined riser circular reaction-regeneration device |
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