CN102875284B - The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha - Google Patents
The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha Download PDFInfo
- Publication number
- CN102875284B CN102875284B CN201110193486.1A CN201110193486A CN102875284B CN 102875284 B CN102875284 B CN 102875284B CN 201110193486 A CN201110193486 A CN 201110193486A CN 102875284 B CN102875284 B CN 102875284B
- Authority
- CN
- China
- Prior art keywords
- riser tube
- settling vessel
- revivifier
- low
- carbon alkene
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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 present invention relates to the reaction unit that low-carbon alkene prepared by a kind of methyl alcohol and petroleum naphtha, mainly solve the problem that in prior art, yield of light olefins is low.The present invention mainly comprises riser tube I7 by adopting, riser tube II12, riser tube III8, settling vessel 17 and revivifier 10, settling vessel 17 and revivifier 10 coaxially arranged, settling vessel 17 is positioned at revivifier 10 top, the entrance end of riser tube I7 and riser tube II12 is positioned at revivifier 10, exit end is positioned at settling vessel 17, it is stripping zone 18 bottom settling vessel 17, bottom, stripping zone 18 has at least two catalyst outlets, one is connected with revivifier 10 by regeneration standpipe 11, one is connected with riser tube III8 by pipeline 9, riser tube III8 and settling vessel 17 are arranged in juxtaposition, riser tube III8 exit end is positioned at settling vessel 17, the technical scheme that settling vessel 17 top has product gas outlet 21 solves the problems referred to above preferably, can be used in the industrial production of low-carbon alkene.
Description
Technical field
The present invention relates to the reaction unit that low-carbon alkene prepared by a kind of 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.
US20070083071 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.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 reaction unit preparing low-carbon alkene with methyl alcohol and petroleum naphtha newly.This device 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 reaction unit of low-carbon alkene prepared by a kind of methyl alcohol and petroleum naphtha, mainly comprise riser tube I7, riser tube II12, riser tube III8, settling vessel 17 and revivifier 10, settling vessel 17 and revivifier 10 coaxially arranged, settling vessel 17 is positioned at revivifier 10 top, the entrance end of riser tube I7 and riser tube II12 is positioned at revivifier 10, exit end is positioned at settling vessel 17, it is stripping zone 18 bottom settling vessel 17, bottom, stripping zone 18 has at least two catalyst outlets, one is connected with revivifier 10 by regeneration standpipe 11, one is connected with riser tube III8 by pipeline 9, riser tube III8 and settling vessel 17 are arranged in juxtaposition, riser tube III8 exit end is positioned at settling vessel 17, settling vessel 17 top has product gas outlet 21.
In technique scheme, described catalyzer comprises ZSM-5 molecular sieve; Described riser tube I7 entrance end is positioned at the degas zone 5 of revivifier 10 bottom, and riser tube II12 entrance end is positioned at the degas zone 25 of revivifier 10 bottom; Described riser tube III8 outlet is arranged slightly revolves 20, slightly revolves 20 gaseous phase outlets and is connected with the entrance of gas-solid cyclone separator 19.
In the present invention, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 10 ~ 100; Described regenerated catalyst coke content massfraction is 0.01 ~ 0.5%; Except petroleum naphtha, also comprise water vapour in described riser tube I7 charging, the weight ratio of water vapour and petroleum naphtha is 0.05 ~ 1.5: 1; The charging of described riser tube II12 is isolated more than the C4 hydrocarbon of centrifugal station; The charging of described riser tube III8 is mainly methyl alcohol; Described petroleum naphtha boiling range is between 20 DEG C ~ 220 DEG C; In described riser tube I7, reaction conditions is: temperature of reaction is 580 ~ 690 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 II12, reaction conditions is: temperature of reaction is 560 ~ 660 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 III8, reaction conditions is: temperature of reaction is 425 ~ 500 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 10 meter per seconds; Catalyzer in described settling vessel 17 is at least divided into two portions after stripping, and 40 ~ 70% enter revivifier 10 regenerates, and 30 ~ 60% enter riser tube III8.
ZSM-5 molecular sieve of the present invention can adopt method known in the field, as hydrothermal synthesis method, be prepared, described molecular sieve catalyst optionally load can have the metal of dehydrogenation functionality, the metal of dehydrogenation functionality is selected from least one in IB, IIB, VB, VIB, VIIB in the periodic table of elements or VIII, and the method for the metal load of dehydrogenation functionality on ZSM-5 molecular sieve can be adopted method known in the field, as pickling process or coprecipitation method.After the ZSM-5 molecular sieve of load dehydrogenation functionality metal prepares, add binding agent, make mixed slurry, adopt spray drying process to carry out drying and moulding, then the catalyst fines after shaping is placed in stoving oven and carries out roasting, after cooling, obtain catalyst sample.Binding agent can select SiO
2, Al
2o
3deng.
Adopt device of the present invention, arrange three riser tubes, it is low-carbon alkene that riser tube I7 is mainly used in convert naphtha, and riser tube II12 is mainly used in transforming more than the C4 hydrocarbon separated, and it is low-carbon alkene that riser tube III8 is used for converting methanol.Riser tube I7 and riser tube II12 main body are positioned at revivifier 10, temperature of reaction is high, regenerated catalyst activity is high, be conducive to the generation low-carbon alkene of petroleum naphtha and more than C4 hydrocarbon high conversion in riser tube, from riser tube I7 and riser tube II12, catalyzer out has a certain amount of carbon distribution, but catalyst activity is still very high, can be further used for methanol conversion is low-carbon alkene, carbon distribution simultaneously on catalyzer can contribute to the raising of selectivity of light olefin, catalyzer simultaneously in settling vessel 17 is through thermo-negative reaction such as high-carbon hydrocarbon cracking, after stripping, the temperature range that can be reduced to preparing olefin by conversion of methanol falls in temperature, what ensure methyl alcohol highly selective is converted into low-carbon alkene.Therefore, adopt device of the present invention, the object improving yield of light olefins can be reached.
Adopt technical scheme of the present invention: described catalyzer comprises ZSM-5 molecular sieve; Described riser tube I7 entrance end is positioned at the degas zone 5 of revivifier 10 bottom, and riser tube II12 entrance end is positioned at the degas zone 25 of revivifier 10 bottom; Described riser tube III8 outlet is arranged slightly revolves 20, and slightly revolve 20 gaseous phase outlets and be connected with the entrance of gas-solid cyclone separator 19, low-carbon alkene carbon base absorption rate can reach 62.19% weight, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of device of the present invention.
In Fig. 1,1 is regenerating medium source line; 2 is plug valve to be generated; 3 is methanol feed line; 4 is riser tube III lower lift section; 5 is degas zone, riser tube I bottom; 6 is naphtha feed pipeline; 7 is riser tube I; 8 is riser tube III; 9 is catalyzer enters riser tube III pipeline from settling vessel; 10 is revivifier; 11 is regeneration standpipe; 12 is riser tube II; 13 is degassed medium inlet pipeline; 14 is stripping fluid source line; 15 is revivifier gas-solid cyclone separator; 16 is exhanst gas outlet; 17 is settling vessel; 18 is stripping zone; 19 is gas-solid cyclone separator; 20 slightly revolve for riser tube III exports; 21 is products export pipeline; 22 is more than C4 hydrocarbon feeding line; 23 is degassed medium inlet pipeline; 24 is overflow weir; 25 is degas zone, riser tube II bottom.
The raw material comprising petroleum naphtha enters riser tube I7, contact with regenerated catalyst, generate the product stream comprising low-carbon alkene and enter settling vessel 17 together with catalyzer, after gas solid separation, product stream enters centrifugal station, and be separated and obtain low-carbon alkene product, isolated more than C4 hydrocarbon enters riser tube II12, contact with regenerated catalyst, generate the product stream comprising low-carbon alkene and enter described settling vessel 17 together with catalyzer; Catalyzer in described settling vessel 17 is at least divided into two portions after stripping, a part enters revivifier 10 through regeneration standpipe 11 and regenerates, the described regenerated catalyst formed enters riser tube I7 and II12, a part enters riser tube III8 through pipeline 9, with the contact raw comprising methyl alcohol, generate the product stream comprising low-carbon alkene and enter described settling vessel 17 together with catalyzer.
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, feed naphtha enters riser tube I7, contact with regenerated catalyst, generate the product stream comprising low-carbon alkene and enter settling vessel 17 together with catalyzer, after gas solid separation, product stream enters centrifugal station, separation obtains low-carbon alkene product, isolated more than C4 hydrocarbon enters riser tube II12, contact with regenerated catalyst, generate the product stream comprising low-carbon alkene and enter described settling vessel 17 together with catalyzer, catalyzer in described settling vessel 17 is divided into two portions after stripping, 40% enters revivifier 10 regenerates, the described regenerated catalyst formed enters riser tube I7 and II12, 60% enters riser tube III8, contact with methanol feedstock, generate the product stream comprising low-carbon alkene and enter described settling vessel 17 together with catalyzer.Settling vessel 17 and revivifier 10 coaxially arranged, settling vessel 17 is positioned at revivifier 10 top, and the entrance end of riser tube I7 and II12 is positioned at revivifier 10, and exit end is positioned at settling vessel 17.Described riser tube I7 entrance end is positioned at the degas zone 5 of revivifier 10 bottom, and riser tube II12 entrance end is positioned at the degas zone 25 of revivifier 10 bottom; Described riser tube III8 outlet is arranged slightly revolves 20, slightly revolves 20 gaseous phase outlets and is connected with the entrance of gas-solid cyclone separator 19.Described catalyzer is ZSM-5, ZSM-5 molecular sieve SiO
2/ Al
2o
3mol ratio is 10, and regenerated catalyst coke content massfraction is 0.01%, also comprises water vapour in riser tube I7 charging, and the weight ratio of water vapour and petroleum naphtha is 0.05: 1, and petroleum naphtha composition is in table 1.In riser tube I7, reaction conditions is: temperature of reaction is 580 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; In riser tube II12, reaction conditions is: temperature of reaction is 560 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; In riser tube III8, reaction conditions is: temperature of reaction is 425 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds.Methyl alcohol and naphtha feed weight ratio are 1: 1.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 53.34% 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, the catalyzer in described settling vessel 17 is divided into two portions after stripping, and 70% enters revivifier 10 regenerates, and 30% enters riser tube III8.ZSM-5 molecular sieve SiO
2/ Al
2o
3mol ratio is 100, and regenerated catalyst coke content massfraction is 0.5%, also comprises water vapour in riser tube I7 charging, and the weight ratio of water vapour and petroleum naphtha is 1.5: 1.In riser tube I7, reaction conditions is: temperature of reaction is 690 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; In riser tube II12, reaction conditions is: temperature of reaction is 660 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; In riser tube III8, reaction conditions is: temperature of reaction is 500 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds.Methyl alcohol and naphtha feed weight ratio are 0.5: 1.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 47.14% weight.
[embodiment 3]
According to the condition described in embodiment 1 and step, the catalyzer in described settling vessel 17 is divided into two portions after stripping, and 50% enters revivifier 10 regenerates, and 50% enters riser tube III.ZSM-5 molecular sieve SiO
2/ Al
2o
3mol ratio is 50, and regenerated catalyst coke content massfraction is 0.1%, also comprises water vapour in riser tube I7 charging, and the weight ratio of water vapour and petroleum naphtha is 0.5: 1.In riser tube I7, reaction conditions is: temperature of reaction is 650 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds; In riser tube II12, reaction conditions is: temperature of reaction is 640 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; In riser tube III8, reaction conditions is: temperature of reaction is 460 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds.Methyl alcohol and naphtha feed weight ratio are 2: 1.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 62.19% weight.
[embodiment 4]
According to the condition described in embodiment 1 and step, the catalyzer in described settling vessel 17 is divided into two portions after stripping, and 50% enters revivifier 10 regenerates, and 50% enters riser tube III8.ZSM-5 molecular sieve SiO
2/ Al
2o
3mol ratio is 70, and regenerated catalyst coke content massfraction is 0.12%, also comprises water vapour in riser tube I7 charging, and the weight ratio of water vapour and petroleum naphtha is 0.5: 1.In riser tube I7, 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 6 meter per seconds; In riser tube II12, reaction conditions is: temperature of reaction is 640 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; In riser tube III8, reaction conditions is: temperature of reaction is 460 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds.Methyl alcohol and naphtha feed weight ratio are 2: 1.Keep the stability of catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 56.24% weight.
[comparative example 1]
According to the condition described in embodiment 3 and step, just do not arrange riser tube II12, low-carbon alkene carbon base absorption rate is 51.49% weight.
[comparative example 2]
According to the condition described in embodiment 3 and step, just do not arrange riser tube II12 and riser tube III8, low-carbon alkene carbon base absorption rate is 37.14% weight.
Obviously, adopt device 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 (4)
1. prepare the reaction unit of low-carbon alkene with methyl alcohol and petroleum naphtha for one kind, mainly comprise riser tube I (7), riser tube II (12), riser tube III (8), settling vessel (17) and revivifier (10), settling vessel (17) and revivifier (10) coaxially arranged, settling vessel (17) is positioned at revivifier (10) top, the entrance end of riser tube I (7) and riser tube II (12) is positioned at revivifier (10), exit end is positioned at settling vessel (17), settling vessel (17) bottom is stripping zone (18), stripping zone (18) bottom has at least two catalyst outlets, one is connected with revivifier (10) by regeneration standpipe (11), one is connected with riser tube III (8) by pipeline (9), riser tube III (8) and settling vessel (17) are arranged in juxtaposition, riser tube III (8) exit end is positioned at settling vessel (17), settling vessel (17) top has product gas outlet (21).
2. prepare the reaction unit of low-carbon alkene according to claim 1 with methyl alcohol and petroleum naphtha, it is characterized in that described catalyzer comprises ZSM-5 molecular sieve.
3. the reaction unit of low-carbon alkene is prepared according to claim 1 with methyl alcohol and petroleum naphtha, it is characterized in that described riser tube I (7) entrance end is positioned at the degas zone (5) of revivifier (10) bottom, riser tube II (12) entrance end is positioned at the degas zone (25) of revivifier (10) bottom.
4. the reaction unit of low-carbon alkene is prepared according to claim 1 with methyl alcohol and petroleum naphtha, it is characterized in that the outlet of described riser tube III (8) is arranged slightly to revolve (20), slightly revolve (20) gaseous phase outlet and be connected with the entrance of gas-solid cyclone separator (19).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193486.1A CN102875284B (en) | 2011-07-12 | 2011-07-12 | The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193486.1A CN102875284B (en) | 2011-07-12 | 2011-07-12 | The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102875284A CN102875284A (en) | 2013-01-16 |
| CN102875284B true CN102875284B (en) | 2015-12-16 |
Family
ID=47476846
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110193486.1A Active CN102875284B (en) | 2011-07-12 | 2011-07-12 | The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102875284B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103212347A (en) * | 2013-04-09 | 2013-07-24 | 张济宇 | High-airspeed riser reactor for preparing light carbon olefin through carbinol and application of high-airspeed riser reactor |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6049017A (en) * | 1998-04-13 | 2000-04-11 | Uop Llc | Enhanced light olefin production |
| CN101941876A (en) * | 2009-07-06 | 2011-01-12 | 中国石油化工股份有限公司上海石油化工研究院 | Method for increasing production of light olefin |
| 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 |
| CN102041032A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Coaxial type compounding lifting pipe circular reaction-regenerating device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020003103A1 (en) * | 1998-12-30 | 2002-01-10 | B. Erik Henry | Fluid cat cracking with high olefins prouduction |
-
2011
- 2011-07-12 CN CN201110193486.1A patent/CN102875284B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6049017A (en) * | 1998-04-13 | 2000-04-11 | Uop Llc | Enhanced light olefin production |
| CN101941876A (en) * | 2009-07-06 | 2011-01-12 | 中国石油化工股份有限公司上海石油化工研究院 | Method for increasing production of light olefin |
| 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 |
| CN102041032A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Coaxial type compounding lifting pipe circular reaction-regenerating device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102875284A (en) | 2013-01-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101333141B (en) | Reaction device for conversing methanol or dimethyl ether to be low carbon olefin | |
| CN102276386A (en) | Production method of light olefins | |
| CN102876363B (en) | Method for catalytically converting naphtha to low-carbon olefins | |
| CN102875299A (en) | Method for producing low-carbon olefins by using methanol and naphtha | |
| CN102875285B (en) | Methyl alcohol and light naphthar are catalytically conveted to the method for low-carbon alkene | |
| CN102276406B (en) | Method for increasing yield of propylene | |
| CN102295510A (en) | Method for catalytically converting naphtha into low-carbon olefin | |
| CN102875289B (en) | Method for preparing low-carbon olefins | |
| CN102295505B (en) | Reaction device for preparing low-carbon olefin from methanol | |
| CN102276404A (en) | Reaction device for producing lower olefins from methanol | |
| CN102276389B (en) | Reaction and regeneration device for catalyzing and converting methanol and naphtha into lower olefins | |
| CN102276391B (en) | Method for catalyzing and converting methanol and naphtha into low-carbon olefins | |
| CN102875283B (en) | The method of low-carbon alkene is prepared by methyl alcohol and petroleum naphtha | |
| CN102875295B (en) | Production method of low-carbon olefins | |
| CN102875288B (en) | Method for producing low-carbon olefins | |
| CN102875284B (en) | The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha | |
| CN102875304B (en) | Method for preparing low carbon olefins from methanol and naphtha | |
| CN102875297B (en) | The method of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha | |
| CN102276399B (en) | Method for producing lower olefins from methanol and naphtha | |
| CN103772089A (en) | Reaction device for improving yield of ethylene and propylene | |
| CN102872761B (en) | Production device of low-carbon olefins | |
| CN103739418B (en) | Improve the method for yield of light olefins in preparing light olefins from methanol technique | |
| CN102875286B (en) | Method for producing low-carbon olefins from methanol and naphtha | |
| CN102875290B (en) | Reaction unit for preparing low-carbon olefins by using methanol and naphtha | |
| CN102875279B (en) | Reaction unit for preparing low-carbon olefins from methanol and naphtha |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |