CN102464557A - Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene - Google Patents
Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene Download PDFInfo
- Publication number
- CN102464557A CN102464557A CN2010105527291A CN201010552729A CN102464557A CN 102464557 A CN102464557 A CN 102464557A CN 2010105527291 A CN2010105527291 A CN 2010105527291A CN 201010552729 A CN201010552729 A CN 201010552729A CN 102464557 A CN102464557 A CN 102464557A
- Authority
- CN
- China
- Prior art keywords
- toluene
- raw material
- ylene
- fluidized
- bed reactor
- 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.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene. The problem that the yield of the dimethylbenzene is lower in the prior art is solved. The method comprises the following steps that: a first part of raw material enters a reactor from the bottom of a fluidized bed reactor, and a second part of raw material enters the reactor from at least one material inlet isolated in the axial direction of the fluidized bed reactor to be in contact with a fluidized bed catalyst to generate a product containing the dimethylbenzene under an effective condition, wherein the density of the bed layer of the fluidized bed reactor is 50 to 500kg/m<3>, the first part of raw material is methylbenzene and water vapor, the weight ratio between the water vapor and the methylbenzene is (0.01-0.2):1, the second part of raw material is a mixture of methanol or dimethyl ether and methylbenzene, and the weight ratio between the methanol or dimethyl ether and the methylbenzene is (1-10):1. The problem is better solved through the technical scheme and the method can be applied to the industrial production of the dimethylbenzene.
Description
Technical field
The present invention relates to a kind ofly prepare the method for YLENE, be particularly useful for preparing the method for p-Xylol by methyl alcohol or dme and toluene by oxygenatedchemicals and toluene.
Background technology
YLENE is important basic raw material, especially p-Xylol.P-Xylol is the basic raw material of synthesizing polyester (PET), and toluene, C are mainly adopted in p-Xylol production at present
9Aromatic hydrocarbons and xylol are raw material, prepare through disproportionation, isomerizing, fractionation by adsorption or low temperature separation process.Because the p-Xylol content in its product receives thermodynamic control, p-Xylol is at C
8Only account for approximately 24% in the BTX aromatics, solid circulating rate is very big in the technological process, and process cost is higher.In recent years, the lot of domestic and international patent discloses a lot of variation routes of preparation p-Xylol, wherein, is paid much attention to through the technology that methylation reaction prepares p-Xylol by methyl alcohol and toluene.Because the boiling point of three isomer differs very little in the YLENE, through the highly purified p-Xylol of the very difficult acquisition of the distillation technique of routine.The selectivity of the raising p-Xylol that therefore need in the process of preparation YLENE, try one's best.
After nineteen seventies ZSM-5 synthesizes successfully,, cause extensive attention because this catalyzer all has unique catalytic performance to many reactions such as alkylation, isomerizing, phenyl ring methylate.The pore canal system that the ZSM-5 zeolite is made up of 10 yuan of rings; Have medium sized aperture and aperture; Can allow molecular diameter is that the p-Xylol of 0.63 nanometer spreads rapidly, can effectively hinder o-Xylol, m-xylene diffusion that molecular diameter is 0.69 nanometer simultaneously.This fact means carries out the possibility that shape is selected to toluene phenyl ring methylation reaction, can obtain to be higher than in the YLENE product p-Xylol content of thermodynamic(al)equilibrium concentration far away.
CN1326430 discloses the method that a kind of alkylated aromatic hydrocarbons reactant is produced alkylation aromatic products, and especially for the methanol toluene methylation reaction, its characteristic mainly is to have adopted the method that toluene, methyl alcohol are introduced reactor drum in different positions to prepare YLENE.CN1355779 discloses the method that a kind of direct selective synthesizing becomes p-Xylol, the aromatic hydroxy compound through will comprising toluene, benzene and composition thereof with by CO, CO
2, H
2And composition thereof the methylating reagent reaction formed, this method makes at least 5% aromatic hydroxy compound be converted into xylene mixture, wherein p-Xylol accounts at least 30% of xylene mixture.
CN1231653 discloses the method that a kind of selectivity is made p-Xylol, and on the catalyzer that a kind of porous crystalline material is processed, this catalyzer comprises the oxide compound that ZSM-5 or ZSM-11 zeolite and modification use, with methyl alcohol and toluene prepared in reaction p-Xylol.CN1775715 discloses a kind of method for preparing the YLENE product, uses a kind of ZSM-5 zeolite ability catalyzer of phosphorous modification, toluene, methyl alcohol, hydrogen are introduced reactor drum, but the toluene conversion in this method is on the low side, and the highest only have 23%.CN1759081 discloses a kind of method for preparing p-Xylol; Adopt the ZSM-5 zeolite catalyst of oxide modifying, in flow reactor, operation under high linear speed; Reactant and catalyzer duration of contact were less than 1 second; Can improve the p-Xylol selectivity, but the toluene conversion of this method is on the low side, the highest only have 22%.
All there is the lower problem of YLENE yield in prior art, and the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the low problem of the p-Xylol yield that exists in the prior art, and a kind of new method that is prepared YLENE by oxygenatedchemicals and toluene is provided.This method is used for the production of p-Xylol, has p-Xylol yield advantage of higher.
For addressing the above problem; The technical scheme that the present invention adopts is following: a kind of method that is prepared YLENE by oxygenatedchemicals and toluene; First part's raw material gets into said reactor drum from the fluidized-bed reactor bottom; The second section raw material gets into reactor drum from least one opening for feed that the fluidized-bed reactor axial direction due separates, and contacts with fluid catalyst, under condition for validity, generates the product that comprises YLENE; Wherein, the fluidized-bed reactor bed density is 50～500 kilograms/meter
3, said first part raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.01～0.2: 1, and the second section raw material is the mixture of methyl alcohol or dme and toluene, and the weight ratio of methyl alcohol or dme and toluene is 1～10: 1.
In the technique scheme, said catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200; Said second section raw material gets into reactor drum from least two opening for feeds that the fluidized-bed reactor axial direction due separates; Said fluidized-bed reactor bed density is 80～200 kilograms/meter
3Said condition for validity is: reaction pressure is counted 0.01～2.0MPa with gauge pressure, and temperature of reaction is 325～500 ℃, and the gas phase linear speed is 0.4～1.8 meter per second, and the average carbon deposition quantity massfraction of catalyzer is 0.1～1.0%.
The method of calculation of average coke content according to the invention are that carbon deposit quality on the catalyzer of certain mass is divided by described catalyst quality.Carbon deposit measuring method on the catalyzer is following: will mix the catalyst mix that has carbon deposit comparatively uniformly; The accurate carbon-bearing catalyzer of weighing certain mass then; Be put in the pyrocarbon analyser and burn; Through the carbonic acid gas quality of infrared analysis burning generation, thereby obtain the carbonaceous amount on the catalyzer.
Toluene conversion of the present invention, methanol conversion, dimethylbenzene selective, p-Xylol selectivity method of calculation are:
Toluene conversion, toluene quality/methylbenzene raw material quality * 100% in the %=100-product;
Methanol conversion, the methanol quality in the %=100-product/methanol feedstock quality * 100%;
Dimethylbenzene selective, the quality of YLENE/methylbenzene raw material quality * 100% in the %=product;
The p-Xylol selectivity, the quality of YLENE * 100% in the quality/product of p-Xylol in the %=product.
ZSM-5 catalyzer of the present invention is to be active main body with the ZSM-5 molecular sieve, adopt add sticker after method spray-dried, the roasting moulding prepare.The sticker that adds can make SiO
2Or Al
2O
3, the add-on of sticker is counted between 10～80% with its per-cent in moulding rear catalyst quality.The catalyzer of moulding for example adopts the ZGK 5 of phenyl methyl ZGK 5 to select the shape processing.
The inventor through increasing the ratio of toluene and oxygenatedchemicals such as methyl alcohol or dme, with effectively reducing the side reaction that methyl alcohol causes, improves the yield of YLENE through discovering.Adopt method of the present invention, in fluidized-bed reactor, because the existence of back-mixing; Help the contact that mixes of methyl alcohol or dme, toluene, methylbenzene raw material at first gets into reactor drum from the bottom, structure toluene environment; Part toluene is adsorbed in the catalyzer duct simultaneously, and the opening for feed that methyl alcohol or dme and part toluene separate from the reactor drum axial direction due gets into reactor drum, contacts with the toluene environment of structure; Increased the ratio of local toluene and oxygenatedchemicals; Effectively reduced the generation of some side reaction, improved YLENE, especially the yield of p-Xylol.
Adopt technical scheme of the present invention: said catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200; Said second section raw material gets into reactor drum from least two opening for feeds that the fluidized-bed reactor axial direction due separates; Said fluidized-bed reactor bed density is 80～200 kilograms/meter
3Said condition for validity is: reaction pressure is counted 0.01～2.0MPa with gauge pressure, and temperature of reaction is 325～500 ℃, and the gas phase linear speed is 0.4～1.8 meter per second; The average carbon deposition quantity massfraction of catalyzer is 0.1～1.0%; Toluene conversion reaches 36%, and methanol conversion reaches 99%, and the p-Xylol selectivity reaches 94%; P-Xylol once through yield based on toluene reaches 34%, has obtained better technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is the fluidized-bed reactor reaction zone; 2 is the opening for feed of reaction zone bottom; 3 is the circulation loop of catalyzer; 4 is the gas solid separation district of fluidized-bed reactor; 5 is cyclonic separator; 6 is fluidized-bed reactor product outlet pipe; 7 for leading to the reclaimable catalyst line of pipes of revivifier; 8 is the inlet on the reaction zone axial direction due; 9 for returning regenerated catalyst the line of pipes of reaction zone.
First part's raw material gets into the reaction zone 1 of fluidized-bed reactor among Fig. 1 through opening for feed 2; Contact with catalyzer; The second section raw material is from being injected into reaction zone 1 along the axially spaced a plurality of inlets 8 of reactor drum; Contact with the catalyzer in the reaction zone 1, reaction generates the logistics that contains YLENE, utilizes the cyclonic separator 5 in the reactor drum gas solid separation district 4 to separate after reactor product outlet pipe 6 gets into follow-up centrifugal station.The catalyzer that reclaims through cyclonic separator 5 returns reaction zone 1 through dipleg.The part of decaying catalyst gets into reaction zone 1 fcc raw material again through the circulation loop 3 of catalyzer in the disengaging zone, helps to adjust the average coke content of reaction zone 1 inner catalyst and the selectivity of reactor bottom reaction.Another part decaying catalyst is all or part of to be sent to breeding blanket regeneration through pipeline 7, and the catalyzer after regeneration is accomplished turns back to reaction zone 1 through pipeline 9.
Through embodiment the present invention is done further elaboration below, but be not limited only to present embodiment.
Embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20; First part's raw material gets into said reactor drum from the fluidized-bed reactor bottom; The second section raw material gets into reactor drum from the opening for feed that the fluidized-bed reactor axial direction due separates, and opening for feed is positioned at apart from 1/3 reaction zone height place, reaction zone bottom, contacts with fluid catalyst; Generation comprises the product of YLENE, and the fluidized-bed reactor bed density is 50 kilograms/meter
3, first part's raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.2: 1, and the second section raw material is the mixture of methyl alcohol and toluene, and the weight ratio of methyl alcohol and toluene is 1: 1.Reaction pressure is counted 0.01MPa with gauge pressure; Temperature of reaction is 325 ℃, and the gas phase linear speed is 1.8 meter per seconds, and the average carbon deposition quantity massfraction of catalyzer is 0.1%; Toluene conversion is 34.15%; Methanol conversion is 88.65%, and dimethylbenzene selective is 75.68%, and the p-Xylol selectivity is 91.53%.
[embodiment 2]
According to embodiment 1 described condition and step, catalyst S iO
2/ Al
2O
3Mol ratio is 200; First part's raw material gets into said reactor drum from the fluidized-bed reactor bottom, and the second section raw material gets into reactor drum from two opening for feeds that the fluidized-bed reactor axial direction due separates, and two opening for feeds lay respectively at apart from 1/3,1/2 reaction zone height place, reaction zone bottom; The inlet amount of two opening for feeds equates; Contact with fluid catalyst, generate the product that comprises YLENE, the fluidized-bed reactor bed density is 80 kilograms/meter
3, first part's raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.1: 1, and the second section raw material is the mixture of methyl alcohol and toluene, and the weight ratio of methyl alcohol and toluene is 2: 1.Reaction pressure is counted 0.01MPa with gauge pressure; Temperature of reaction is 350 ℃, and the gas phase linear speed is 1.5 meter per seconds, and the average carbon deposition quantity massfraction of catalyzer is 0.14%; Toluene conversion is 34.96%; Methanol conversion is 93.64%, and dimethylbenzene selective is 76.82%, and the p-Xylol selectivity is 92.09%.
[embodiment 3]
According to embodiment 1 described condition and step, catalyst S iO
2/ Al
2O
3Mol ratio is 100; First part's raw material gets into said reactor drum from the fluidized-bed reactor bottom, and the second section raw material gets into reactor drum from three opening for feeds that the fluidized-bed reactor axial direction due separates, and three opening for feeds lay respectively at apart from 1/4,1/2,2/3 reaction zone height place, reaction zone bottom; The inlet amount of three opening for feeds equates; Contact with fluid catalyst, generate the product that comprises YLENE, the fluidized-bed reactor bed density is 200 kilograms/meter
3, first part's raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.01: 1, and the second section raw material is the mixture of methyl alcohol and toluene, and the weight ratio of methyl alcohol and toluene is 10: 1.Reaction pressure is counted 0.01MPa with gauge pressure; Temperature of reaction is 400 ℃, and the gas phase linear speed is 0.9 meter per second, and the average carbon deposition quantity massfraction of catalyzer is 0.96%; Toluene conversion is 35.86%; Methanol conversion is 97.13%, and dimethylbenzene selective is 80.54%, and the p-Xylol selectivity is 94.17%.
[embodiment 4]
According to embodiment 3 described condition and steps, the fluidized-bed reactor bed density is 500 kilograms/meter
3, first part's raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.01: 1, and the second section raw material is the mixture of dme and toluene, and the weight ratio of dme and toluene is 10: 1.Reaction pressure is counted 2.0MPa with gauge pressure; Temperature of reaction is 500 ℃, and the gas phase linear speed is 0.4 meter per second, and the average carbon deposition quantity massfraction of catalyzer is 0.12%; Toluene conversion is 36.29%; Methanol conversion is 99.57%, and dimethylbenzene selective is 85.04%, and the p-Xylol selectivity is 92.07%.
[embodiment 5]
According to embodiment 4 described condition and steps, the fluidized-bed reactor bed density is 400 kilograms/meter
3, first part's raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.1: 1, and the second section raw material is the mixture of methyl alcohol, dme and toluene, and the weight ratio of methyl alcohol, dme and toluene is 5: 10: 1.Reaction pressure is counted 0.3MPa with gauge pressure; Temperature of reaction is 450 ℃, and the gas phase linear speed is 0.7 meter per second, and the average carbon deposition quantity massfraction of catalyzer is 0.32%; Toluene conversion is 35.79%; Methanol conversion is 99.41%, and dimethylbenzene selective is 85.77%, and the p-Xylol selectivity is 93.76%.
Obviously, adopt method of the present invention, can reach the purpose that improves the p-Xylol yield, have bigger technical superiority, can be used in the industrial production of YLENE.
Claims (5)
1. method for preparing YLENE by oxygenatedchemicals and toluene; First part's raw material gets into said reactor drum from the fluidized-bed reactor bottom; The second section raw material gets into reactor drum from least one opening for feed that the fluidized-bed reactor axial direction due separates; Contact with fluid catalyst, under condition for validity, generate the product that comprises YLENE; Wherein, the fluidized-bed reactor bed density is 50～500 kilograms/meter
3, said first part raw material is toluene and water vapour, and the weight ratio of water vapour and toluene is 0.01～0.2: 1, and the second section raw material is the mixture of methyl alcohol or dme and toluene, and the weight ratio of methyl alcohol or dme and toluene is 1～10: 1.
2. prepare the method for YLENE according to claim 1 is said by oxygenatedchemicals and toluene, it is characterized in that said catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 20～200.
3. prepare the method for YLENE according to claim 1 is said by oxygenatedchemicals and toluene, it is characterized in that said second section raw material gets into reactor drums from least two opening for feeds that the fluidized-bed reactor axial direction due separates.
4. prepare the method for YLENE according to claim 1 is said by oxygenatedchemicals and toluene, it is characterized in that said fluidized-bed reactor bed density is 80～200 kilograms/meter
3
5. according to the said method for preparing YLENE by oxygenatedchemicals and toluene of claim 1; It is characterized in that said condition for validity is: reaction pressure is counted 0.01～2.0MPa with gauge pressure; Temperature of reaction is 325～500 ℃; The gas phase linear speed is 0.4～1.8 meter per second, and the average carbon deposition quantity massfraction of catalyzer is 0.1～1.0%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010552729.1A CN102464557B (en) | 2010-11-17 | 2010-11-17 | Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010552729.1A CN102464557B (en) | 2010-11-17 | 2010-11-17 | Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102464557A true CN102464557A (en) | 2012-05-23 |
| CN102464557B CN102464557B (en) | 2014-03-26 |
Family
ID=46068722
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010552729.1A Active CN102464557B (en) | 2010-11-17 | 2010-11-17 | Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102464557B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103588601A (en) * | 2013-11-13 | 2014-02-19 | 上海华谊（集团）公司 | Fluidized bed method for producing p-xylene through shape-selective toluene and methanol alkylation |
| WO2018196363A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and benzene |
| WO2018196360A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Device and method for preparing para-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and toluene |
| WO2018196364A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Apparatus and method for preparing para-xylene co-producing low-carbon olefin from methanol and/or dimethyl ether and benzene |
| CN108794294A (en) * | 2017-04-27 | 2018-11-13 | 中国科学院大连化学物理研究所 | Gas distributor of fludized bed, using its reactor and produce paraxylene co-producing light olefins method |
| CN108786669A (en) * | 2017-04-27 | 2018-11-13 | 中国科学院大连化学物理研究所 | Gas distributor of fludized bed, using its reactor and produce paraxylene co-producing light olefins method |
| CN109395674A (en) * | 2018-12-20 | 2019-03-01 | 清华大学 | Alcohol/ether/C3-C5 hydrocarbon directly prepares paraxylene reactor and method |
| KR20190140467A (en) * | 2017-04-27 | 2019-12-19 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the preparation of paraxylene with methanol and / or dimethylether and toluene and the simultaneous production of low carbon olefins |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3751504A (en) * | 1972-05-12 | 1973-08-07 | Mobil Oil Corp | Vapor-phase alkylation in presence of crystalline aluminosilicate catalyst with separate transalkylation |
| US4377718A (en) * | 1980-07-25 | 1983-03-22 | Teijin Petrochemical Industries Ltd. | Process for producing p-xylene |
| CN1326430A (en) * | 1998-10-05 | 2001-12-12 | 美孚石油公司 | Fluid-bed aromatics alkylation |
| CN1404463A (en) * | 2000-02-22 | 2003-03-19 | 埃克森美孚化学专利公司 | Conversion of oxygenate to olefins with staged injection of oxygenate |
-
2010
- 2010-11-17 CN CN201010552729.1A patent/CN102464557B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3751504A (en) * | 1972-05-12 | 1973-08-07 | Mobil Oil Corp | Vapor-phase alkylation in presence of crystalline aluminosilicate catalyst with separate transalkylation |
| US4377718A (en) * | 1980-07-25 | 1983-03-22 | Teijin Petrochemical Industries Ltd. | Process for producing p-xylene |
| CN1326430A (en) * | 1998-10-05 | 2001-12-12 | 美孚石油公司 | Fluid-bed aromatics alkylation |
| CN1404463A (en) * | 2000-02-22 | 2003-03-19 | 埃克森美孚化学专利公司 | Conversion of oxygenate to olefins with staged injection of oxygenate |
Cited By (35)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103588601A (en) * | 2013-11-13 | 2014-02-19 | 上海华谊（集团）公司 | Fluidized bed method for producing p-xylene through shape-selective toluene and methanol alkylation |
| CN108794294B (en) * | 2017-04-27 | 2020-12-11 | 中国科学院大连化学物理研究所 | Fluidized bed gas distributor, reactor using same and method for co-producing p-xylene and low-carbon olefin |
| KR20190138870A (en) * | 2017-04-27 | 2019-12-16 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Apparatus and method for producing paraxylene with methanol and / or dimethyl ether and toluene and simultaneous production of low carbon olefins |
| WO2018196364A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Apparatus and method for preparing para-xylene co-producing low-carbon olefin from methanol and/or dimethyl ether and benzene |
| CN108794294A (en) * | 2017-04-27 | 2018-11-13 | 中国科学院大连化学物理研究所 | Gas distributor of fludized bed, using its reactor and produce paraxylene co-producing light olefins method |
| EP3628397A4 (en) * | 2017-04-27 | 2021-01-06 | Dalian Institute Of Chemical Physics, Chinese Academy of Sciences | Device and method for preparing para-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and toluene |
| US11311852B2 (en) | 2017-04-27 | 2022-04-26 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene |
| KR20190137914A (en) * | 2017-04-27 | 2019-12-11 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed gas distributor, reactor and paraxylene production and simultaneous production of low carbon olefins using the same |
| CN108786669B (en) * | 2017-04-27 | 2021-01-12 | 中国科学院大连化学物理研究所 | Fluidized bed gas distributor, reactor using same and method for co-producing p-xylene and low-carbon olefin |
| KR20190140018A (en) * | 2017-04-27 | 2019-12-18 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed reactor and process for the production of paraxylene with benzene and methanol and / or dimethyl ether and for the simultaneous production of low carbon olefins |
| EP3617178A4 (en) * | 2017-04-27 | 2021-01-27 | Dalian Institute Of Chemical Physics, Chinese Academy of Sciences | Fluidized bed apparatus and method for preparing para-xylene co-produced low-carbon olefin from methanol and/or dimethyl ether and toluene |
| KR20190140467A (en) * | 2017-04-27 | 2019-12-19 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the preparation of paraxylene with methanol and / or dimethylether and toluene and the simultaneous production of low carbon olefins |
| EP3616782A4 (en) * | 2017-04-27 | 2020-05-13 | Dalian Institute Of Chemical Physics, Chinese Academy of Sciences | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and benzene |
| JP2020517589A (en) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Fluidized bed apparatus and method for producing para-xylene from methanol and/or dimethyl ether and toluene and co-producing lower olefins |
| JP2020517596A (en) * | 2017-04-27 | 2020-06-18 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Fluidized bed apparatus and method for producing para-xylene from methanol and/or dimehil ether and benzene and co-producing lower olefins |
| JP2020521621A (en) * | 2017-04-27 | 2020-07-27 | 中国科学院大▲連▼化学物理研究所Ｄａｌｉａｎ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｃｈｅｍｉｃａｌ Ｐｈｙｓｉｃｓ，Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Apparatus and method for producing para-xylene from methanol and/or dimethyl ether and toluene and co-producing lower olefins |
| WO2018196363A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and benzene |
| CN108786669A (en) * | 2017-04-27 | 2018-11-13 | 中国科学院大连化学物理研究所 | Gas distributor of fludized bed, using its reactor and produce paraxylene co-producing light olefins method |
| WO2018196360A1 (en) * | 2017-04-27 | 2018-11-01 | 中国科学院大连化学物理研究所 | Device and method for preparing para-xylene and co-producing low-carbon olefins from methanol and/or dimethyl ether and toluene |
| KR20190140469A (en) * | 2017-04-27 | 2019-12-19 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Apparatus and method for the preparation of paraxylene with methanol and / or dimethylether and benzene and the simultaneous preparation of low carbon olefins |
| RU2743135C1 (en) * | 2017-04-27 | 2021-02-15 | Далянь Инститьют Оф Кемикал Физикс, Чайниз Академи Оф Сайенсиз | Fluidised bed device and a method of producing para-xylene and co-producing lower olefins from methanol and/or dimethyl ether and benzene |
| EP3616783A4 (en) * | 2017-04-27 | 2021-02-17 | Dalian Institute Of Chemical Physics, Chinese Academy of Sciences | Fluidized bed gas distributor, reactor using fluidized bed gas distributor, and method for producing para-xylene and co-producing low-carbon olefins |
| US10967350B2 (en) | 2017-04-27 | 2021-04-06 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Fluidized bed gas distributor, reactor using fluidized bed gas distributor, and method for producing para-xylene and co-producing light olefins |
| US11072571B2 (en) | 2017-04-27 | 2021-07-27 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Fluidized bed reactor and method for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether |
| KR102287015B1 (en) * | 2017-04-27 | 2021-08-06 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed gas distributor, reactor using same, and method for simultaneous production of para-xylene and low-carbon olefin |
| US11084765B2 (en) | 2017-04-27 | 2021-08-10 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene |
| RU2743135C9 (en) * | 2017-04-27 | 2021-08-12 | Далянь Инститьют Оф Кемикал Физикс, Чайниз Академи Оф Сайенсиз | Fluidised bed device and a method of producing para-xylene and co-producing lower olefins from methanol and/or dimethyl ether and benzene |
| KR102309241B1 (en) | 2017-04-27 | 2021-10-05 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Apparatus and method for simultaneous production of para-xylene and low-carbon olefin using methanol and/or dimethyl ether and toluene |
| KR102309237B1 (en) | 2017-04-27 | 2021-10-05 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Apparatus and method for the simultaneous production of low-carbon olefins and the production of para-xylene with methanol and/or dimethyl ether and benzene |
| KR102309238B1 (en) | 2017-04-27 | 2021-10-06 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed apparatus and method for the simultaneous production of low-carbon olefins and the production of para-xylene with methanol and/or dimethyl ether and toluene |
| US11161085B2 (en) | 2017-04-27 | 2021-11-02 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Fluidized bed device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene |
| KR102325164B1 (en) * | 2017-04-27 | 2021-11-10 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Fluidized bed reactor and production method for the simultaneous production of para-xylene and low-carbon olefins with benzene and methanol and/or dimethyl ether |
| US11180431B2 (en) | 2017-04-27 | 2021-11-23 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Fluidized bed device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene |
| JP7049361B2 (en) | 2017-04-27 | 2022-04-06 | 中国科学院大▲連▼化学物理研究所 | Equipment and methods for producing para-xylene from methanol and / or dimethyl ether and toluene and co-producing lower olefins |
| CN109395674A (en) * | 2018-12-20 | 2019-03-01 | 清华大学 | Alcohol/ether/C3-C5 hydrocarbon directly prepares paraxylene reactor and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102464557B (en) | 2014-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102464557B (en) | Method for preparing dimethylbenzene from oxygen-containing compound and methylbenzene | |
| CN102463086B (en) | Reaction device for co-producing low-carbon olefin and p-xylene | |
| CN101157593B (en) | Method for producing light olefins by methanol or/and dimethyl ether | |
| CN102463084B (en) | Reaction device for preparing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| KR20190138870A (en) | Apparatus and method for producing paraxylene with methanol and / or dimethyl ether and toluene and simultaneous production of low carbon olefins | |
| CN102464550B (en) | Method for co-producing low carbon olefin and paraxylene | |
| CN102464532B (en) | Method for preparing low-carbon olefins | |
| CN102276386A (en) | Production method of light olefins | |
| CN102463138B (en) | Two-stage regeneration method for SAPO-34 catalysts | |
| CN102464529A (en) | Method for increasing yield of low-carbon olefins | |
| CN102190548A (en) | Method for enhancing yield of light olefins in MTO technology | |
| CN102875317B (en) | Method for producing p-xylene | |
| CN102463072B (en) | Reaction device for producing p-xylene | |
| CN102190542B (en) | The coupling process of methanol-to-olefins and carbon more than four hydrocarbon catalytic pyrolysis | |
| CN102464549B (en) | Method for producing propylene and p-xylene | |
| CN102464524A (en) | Method for producing low-carbon olefins from methanol | |
| CN102875318B (en) | Reaction-regeneration device for producing p-xylene | |
| CN102463085B (en) | Reaction device for producing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| CN102464522A (en) | Method for producing low-carbon olefins | |
| CN102464561B (en) | Methanol or dimethyl ether and method for preparing dimethylbenzene by using methylbenzene | |
| CN102190538A (en) | Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol | |
| CN102464526A (en) | Method for producing low-carbon olefins from methanol | |
| CN102464558B (en) | Method for producing paraxylene | |
| CN102464528A (en) | Method for increasing yields of ethylene and propylene | |
| CN102463079A (en) | Reaction device for producing low-carbon olefin from methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |