CN102190538B - Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol - Google Patents
Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol Download PDFInfo
- Publication number
- CN102190538B CN102190538B CN201010116399.1A CN201010116399A CN102190538B CN 102190538 B CN102190538 B CN 102190538B CN 201010116399 A CN201010116399 A CN 201010116399A CN 102190538 B CN102190538 B CN 102190538B
- Authority
- CN
- China
- Prior art keywords
- reaction
- reaction zone
- carbon
- catalyzer
- catalyst
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a method for catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in a process of preparing olefins from methanol, which mainly solves the problem of low yield of light olefins in the prior art. The method for catalytic pyrolysis of the hydrocarbons with more than 4 carbon atoms in the process of preparing olefins from methanol mainly comprises the following steps of: (1) making a methanol-containing raw material enter a main reactor reaction area to contact a silicoaluminophosphate molecular sieve-containing catalyst to obtain a light olefin-containing product flow I and the inactivated catalyst; (2) making the inactivated catalyst enter a regenerator for regeneration, making the regenerated catalyst enter a riser reaction area to contact a raw material containing hydrocarbons with more than 4 carbon atoms, and making the generated products and the catalyst pass through a catalyst buffer fluidization area and enter the riser reaction area to contact the raw material containing the hydrocarbons with more than 4 carbon atoms so as to obtain a light olefin-containing product flow II and the pre-coked catalyst; and (3) performing gas-solid separation on the product flow II, mixing with the product flow I, making the mixture enter a separation section, and returning the pre-coked catalyst to the main reactor reaction area. The adopted technical scheme better solves the problem, and the method can be used for industrial production of light olefins.
Description
Technical field
The present invention relates to the above hydrocarbon catalytic cracking method of carbon four in a kind of MTO technology.
Technical background
Low-carbon alkene, i.e. ethene and propylene, is two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology of alternative materials conversion 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, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to the popularity in oxygenatedchemicals source, add and transform the economy that generates 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).
In US4499327 patent, silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in detail, think that SAPO-34 is the first-selected catalyzer of MTO technique.SAPO-34 catalyzer has very high light olefin selectivity, and activity is also higher, and can make methanol conversion is reaction times of light olefin to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser tube.
Technology and reactor that a kind of oxygenate conversion is low-carbon alkene in US6166282, are announced, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, rise to after the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation 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, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.
In CN1723262, having announced with the multiple riser reaction unit of central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactors, 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.
In Chinese invention patent 200810043971.9, announce a kind of method that improves yield of light olefins, the first top, reaction zone that it is low-carbon alkene in methanol conversion that the method adopts arranges a second reaction zone, and this second reaction zone diameter is greater than the first reaction zone, the residence time with the gas product that increases by the first reaction zone outlet in second reaction zone, make unreacted methyl alcohol, the above hydrocarbon of the dme generating and carbon four continues reaction, reach the object that improves yield of light olefins, the method also comprises that the charging of second reaction zone can be the above hydrocarbon of freshening carbon four through separating.Although the method can improve the yield of low-carbon alkene to a certain extent, but because the first reaction zone catalyzer is out with more carbon distribution, and the above hydrocarbon pyrolysis of carbon four needs higher catalyst activity, therefore in the method, the above hydrocarbon changing effect of the carbon four in second reaction zone is still on the low side.
Therefore, need a kind of novel method, make the above hydrocarbon of carbon four object that is converted into low-carbon alkene how as far as possible to reach, finally reach the object that improves yield of light olefins and process economy.The present invention has solved the problems referred to above targetedly.
Summary of the invention
Technical problem to be solved by this invention is the not high problem of yield of light olefins existing in prior art, and the above hydrocarbon catalytic cracking method of carbon four in a kind of new MTO technology is provided.The method, for the production of low-carbon alkene, has advantages of the more high and low carbon olefin production technique of yield of light olefins better economy.
For addressing the above problem, the technical solution used in the present invention is as follows: the above hydrocarbon catalytic cracking method of carbon four in a kind of MTO technology, mainly comprise the following steps: (1) comprises that the raw material of methyl alcohol enters main reactor reaction zone, contact with comprising silicoaluminophosphamolecular molecular sieve catalyst, generation comprises the product stream I of low-carbon alkene, forms the catalyzer of inactivation simultaneously; (2) catalyzer of described inactivation enters revivifier regeneration, the catalyzer of having regenerated enters down-flow fluidized bed using ECT reaction zone, contact with the raw material that comprises carbon four above hydrocarbon, the product and the catalyzer that generate enter riser reaction zone, contact with the raw material that comprises carbon four above hydrocarbon, generation comprises the product stream II of low-carbon alkene, forms the catalyzer of pre-carbon deposit simultaneously; (3) described product stream II is mixed into centrifugal station with product stream I after gas solid separation, and the catalyzer of described pre-carbon deposit returns to main reactor reaction zone.
In technique scheme, described silicoaluminophosphamolecular molecular sieves is selected from least one in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56, and preferred version is SAPO-34; Temperature of reaction in described main reactor reaction zone is 400～500 ℃, preferred version is 430～480 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 0.8～2.5 meter per second, and preferred version is 1.0～1.5 meter per seconds; Temperature of reaction in down-flow fluidized bed using ECT reaction zone is 510～650 ℃, preferred version is 550～600 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 5.0～15.0 meter per seconds, and preferred version is 7.0～10.0 meter per seconds; Temperature of reaction in riser reaction zone is 500～630 ℃, preferred version is 530～580 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 3.0～10.0 meter per seconds, and preferred version is 5.0～7.0 meter per seconds; The carbon deposition quantity of the catalyzer of described pre-carbon deposit is 0.1～1.8% weight, and preferred version is 0.5～1.2% weight.
The preparation method of silicoaluminophosphamolecular molecular sieve of the present invention is: first preparing molecular sieve presoma, is 0.03～0.6R by mole proportioning: (Si 0.01～0.98: Al 0.01～0.6: P 0.01～0.6): 2～500 H
2o, wherein R represents template, constitutive material mixed solution obtains at a certain temperature after the crystallization of certain hour; Again, molecular sieve presoma, phosphorus source, silicon source, aluminium source, organic formwork agent, water etc. are mixed according to certain ratio after at 110～260 ℃ hydrothermal crystallizing after at least 0.1 hour, finally obtain SAPO molecular sieve.
The molecular sieve of preparation is mixed with a certain proportion of binding agent, after the operation stepss such as, roasting dry through spraying, obtain final SAPO catalyzer, the weight percentage of binding agent in molecular sieve is generally between 10～90%.
In the method for the invention, be provided with three reaction zones, main reactor reaction zone is relatively independent, for preparing olefin by conversion of methanol, down-flow fluidized bed using ECT reaction zone and riser reaction zone series connection, for transforming the above hydrocarbon of carbon four and methyl alcohol or dme etc. for reaction, reach the object that improves feed stock conversion and yield of light olefins.Wherein, down-flow fluidized bed using ECT reaction zone is except having guaranteed the enough reaction times, also because the characteristic of approximate gas-solid plug flow, reduce the occurrence probability of side reaction, the significantly selectivity of low-carbon alkene, the above hydrocarbon of maximized conversion carbon four is low-carbon alkene, and in addition, the parameters such as its material level, temperature of reaction can independently be controlled.And catalyzer in down-flow fluidized bed using ECT reaction zone is directly from revivifier, the activity of the temperature of carrying and catalyzer self is all higher, is conducive to the conversion of the above hydrocarbon of carbon four to low-carbon alkene.In addition, regenerated catalyst passes through behind down-flow fluidized bed using ECT reaction zone and riser reaction zone, after reaction, can accumulate a certain amount of carbon deposit, the inventor finds by research, the above hydrocarbon of carbon four is converted into a certain amount of carbon distribution being accumulated on catalyzer in low carbon olefin hydrocarbon and is conducive to improve the selectivity that methanol conversion is low-carbon alkene, so return behind main reactor reaction zone with the catalyzer of a certain amount of carbon distribution when this part, can obviously improve the selectivity of light olefin in main reactor reaction zone.Simultaneously, because the above hydrocarbon pyrolysis of carbon four is that low-carbon alkene is strong endothermic reaction, the heat of the catalyst entrainment after therefore having reacted in down-flow fluidized bed using ECT reaction zone and riser reaction zone declines, and returns behind main reactor reaction zone, the heat-obtaining load that has alleviated main reactor reaction zone, has effectively utilized heat.Therefore, adopt described method of the present invention, both effectively improved the yield of object product low-carbon alkene, optimized again energy distribution and utilization.
Adopt technical scheme of the present invention: described silicoaluminophosphamolecular molecular sieves is selected from least one in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56; Temperature of reaction in described main reactor reaction zone is 400～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 0.8～2.5 meter per second; Temperature of reaction in down-flow fluidized bed using ECT reaction zone is 510～650 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 5.0～15.0 meter per seconds; Temperature of reaction in riser reaction zone is 500～630 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 3.0～10.0 meter per seconds; The carbon deposition quantity of the catalyzer of described pre-carbon deposit is 0.1～1.8% weight, and selectivity of light olefin can reach 91.24% weight, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is main reactor reaction zone bottom feed; 2 is main reactor reaction zone; 3 is gas-solid sharp separation equipment; 4 is stripping stage; 5 return to the line of pipes of main reactor reaction zone for stripping stage catalyzer; 6 is reclaimable catalyst inclined tube; 7 is main reactor reaction zone external warmer; 8 is gas-solid cyclone separator; 9 is reactor gas solid separation district; 10 is collection chamber; 11 is reactor product outlet line; 12 is revivifier gas solid separation district; 13 is regenerating medium source line; 14 is revivifier breeding blanket; 15 is external catalyst cooler for regenerator; 16 is revivifier gas-solid cyclone separator; 17 is regenerated flue gas outlet line; 18 is regenerated catalyst inclined tube; 19 is riser reaction zone charging; 20 is buffering mixing zone, bottom, riser reaction zone; 21 is riser reaction zone; 22 is gas-solid separation equipment; 23 is catalyzer buffering fluidization regions; 24 is down-flow fluidized bed using ECT reaction zone; 25 is catalyzer buffering fluidization regions bottom feed; 26 is catalyzer buffering fluidization regions its top feed.
Raw material enters in main reactor reaction zone 2 through feeding line 1, contact with molecular sieve catalyst, reaction generates the product stream I that contains low-carbon alkene, after gas-solid sharp separation equipment 3, enters gas solid separation district 9, and decaying catalyst enters revivifier regeneration from reclaimable catalyst inclined tube 6.Catalyzer after having regenerated enters down-flow fluidized bed using ECT reaction zone 24 from regenerated catalyst inclined tube 18 behind catalyzer buffering fluidization regions 23, after contacting with from the raw material of pipeline 25,26, enter riser reaction zone 21, contact with the raw material that comprises carbon four above hydrocarbon, generate low-carbon alkene product stream II, the product that riser reaction zone 21 exports with catalyzer after gas-solid separation equipment 22 separates, in product introduction reactor disengaging zone 9, after mixing with product stream I, enter centrifugal station from outlet line 11.In riser reaction zone 21, reacted catalyzer returns main reactor reaction zone 2 from pipeline 5.
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, main reactor reaction zone medial temperature is 480 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds; Down-flow fluidized bed using ECT reaction zone medial temperature is 550 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 10.0 meter per seconds; Riser reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 5.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 0.5% weight.Main reactor reaction zone bottom feed is pure methyl alcohol, and charging is 2 kgs/hr, and catalyzer is SAPO-34, wherein SiO in molecular sieve
2: Al
2o
3: P
2o
5=0.1: 1: 1, in catalyzer, binder content was 60%.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 87%, down-flow fluidized bed using ECT reaction zone its top feed is identical with riser reaction zone bottom feed, keep the stability of catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 87.51% weight.
[embodiment 2]
According to the condition described in embodiment 1, main reactor reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 2.5 meter per seconds; Down-flow fluidized bed using ECT reaction zone medial temperature is 650 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 15.0 meter per seconds; Riser reaction zone medial temperature is 630 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 10.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 1.8% weight.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 58%, and the stability of maintenance catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 84.27% weight.
[embodiment 3]
According to the condition described in embodiment 1, main reactor reaction zone medial temperature is 400 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 0.8 meter per second; Down-flow fluidized bed using ECT reaction zone medial temperature is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 5.0 meter per seconds; Riser reaction zone medial temperature is 530 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 7.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 0.1% weight.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 84.76% weight.
[embodiment 4]
According to the condition described in embodiment 1, main reactor reaction zone medial temperature is 430 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 1.0 meter per seconds; Down-flow fluidized bed using ECT reaction zone medial temperature is 510 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 10.0 meter per seconds; Riser reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 3.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 1.2% weight.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 86.71% weight.
[embodiment 5]
According to the condition described in embodiment 1, main reactor reaction zone linear gas velocity is 1.2 meter per seconds; Down-flow fluidized bed using ECT reaction zone medial temperature is 600 ℃; Riser reaction zone medial temperature is 580 ℃.The carbon deposition quantity of pre-carbon deposition catalyst is 0.8% weight.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 95%, and the stability of maintenance catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 88.41% weight.
[embodiment 6]
According to the condition described in embodiment 5, down-flow fluidized bed using ECT reaction zone its top feed is mixed c 4, C 4 olefin content 75%, riser reaction zone bottom feed is mixed c 4, C 4 olefin content 95%, the stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 88.46% weight.
[embodiment 7]
According to the condition described in embodiment 5, riser reaction zone bottom feed is mixed c 4 and methyl alcohol, and the olefin(e) centent in mixed c 4 is 95%, and the weight ratio of mixed c 4 and methyl alcohol is 3: 1.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 91.24% weight.
[embodiment 8～11]
According to the condition described in embodiment 1, just change the type of molecular sieve in catalyzer, experimental result is in table 1.
Table 1
| Parameter | Molecular sieve type | Yield of light olefins, % (weight) |
| Embodiment 8 | SAPO-20 | 78.67 |
| Embodiment 9 | SAPO-18 | 86.09 |
| Embodiment 10 | SAPO-56 | 69.86 |
| Embodiment 11 | SAPO-34+SAPO-18 (weight ratio is 2: 1) | 87.79 |
[embodiment 12]
According to the condition described in embodiment 1, SiO in molecular sieve
2: Al
2o
3: P
2o
5=0.2: 1: 1, in catalyzer, binder content was 70%, light olefin carbon base absorption rate is 85.32% (weight).
[comparative example 1]
According to the condition described in embodiment 1, do not establish down-flow fluidized bed using ECT reaction zone and riser reaction zone, regenerated catalyst directly turns back to the bottom of main reactor reaction zone, and low-carbon alkene carbon base absorption rate is 79.5% weight.
Obviously, adopt method of the present invention, can reach the object that improves yield of light olefins, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (4)
1. the above hydrocarbon catalytic cracking method of carbon four in MTO technology, mainly comprises the following steps:
(1) raw material that comprises methyl alcohol enters main reactor reaction zone, contacts with comprising silicoaluminophosphamolecular molecular sieve catalyst, generates the product stream I that comprises low-carbon alkene, forms the catalyzer of inactivation simultaneously;
(2) catalyzer of described inactivation enters revivifier regeneration, the catalyzer of having regenerated enters down-flow fluidized bed using ECT reaction zone, contact with the raw material that comprises carbon four above hydrocarbon, the product and the catalyzer that generate enter riser reaction zone, contact with the raw material that comprises carbon four above hydrocarbon, generation comprises the product stream II of low-carbon alkene, forms the catalyzer of pre-carbon deposit simultaneously;
(3) described product stream II is mixed into centrifugal station with product stream I after gas solid separation, and the catalyzer of described pre-carbon deposit returns to main reactor reaction zone;
Described silicoaluminophosphamolecular molecular sieves is selected from least one in SAPO-5, SAPO-11, SAPO-18, SAPO-34, SAPO-44;
The carbon deposition quantity of the catalyzer of described pre-carbon deposit is 0.5～1.2% weight.
2. the above hydrocarbon catalytic cracking method of carbon four in MTO technology according to claim 1, is characterized in that described silicoaluminophosphamolecular molecular sieves is selected from SAPO-34.
3. the above hydrocarbon catalytic cracking method of carbon four in MTO technology according to claim 1, it is characterized in that the temperature of reaction in described main reactor reaction zone is 400～500 ℃, reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 0.8～2.5 meter per second; Temperature of reaction in down-flow fluidized bed using ECT reaction zone is 510～650 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 5.0～15.0 meter per seconds; Temperature of reaction in riser reaction zone is 500～630 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 3.0～10.0 meter per seconds.
4. the above hydrocarbon catalytic cracking method of carbon four in MTO technology according to claim 3, it is characterized in that the temperature of reaction in described main reactor reaction zone is 430～480 ℃, reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 1.0～1.5 meter per seconds; Temperature of reaction in down-flow fluidized bed using ECT reaction zone is 550～600 ℃, and reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 7.0～10.0 meter per seconds; Temperature of reaction in riser reaction zone is 530～580 ℃, and reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 5.0～7.0 meter per seconds.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010116399.1A CN102190538B (en) | 2010-03-03 | 2010-03-03 | Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010116399.1A CN102190538B (en) | 2010-03-03 | 2010-03-03 | Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102190538A CN102190538A (en) | 2011-09-21 |
| CN102190538B true CN102190538B (en) | 2014-07-02 |
Family
ID=44599505
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010116399.1A Active CN102190538B (en) | 2010-03-03 | 2010-03-03 | Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102190538B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107529620A (en) * | 2017-06-08 | 2018-01-02 | 内蒙古中煤蒙大新能源化工有限公司 | The analysis method of carbonyls in a kind of product of methanol-to-olefins device carbon four |
| CN111423302B (en) * | 2019-01-09 | 2023-09-19 | 国家能源投资集团有限责任公司 | Method and device for preparing olefin from methanol |
| CN112774735A (en) * | 2019-11-09 | 2021-05-11 | 洛阳维达石化工程有限公司 | Method and equipment for pre-hydrocarbon pooling of catalyst |
| CN115304442A (en) * | 2021-05-08 | 2022-11-08 | 国家能源投资集团有限责任公司 | Preparation of C from methanol 2 -C 3 Process and apparatus for olefins |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4499327A (en) * | 1982-10-04 | 1985-02-12 | Union Carbide Corporation | Production of light olefins |
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101165018A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene |
| CN101318869A (en) * | 2008-06-12 | 2008-12-10 | 中国石油化工股份有限公司 | Process for converting oxygen-containing compound to prepare low carbon olefin hydrocarbon |
| CN101348404A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for improving ethylene and propene yield in methyl alcohol or dimethyl ether conversion process |
-
2010
- 2010-03-03 CN CN201010116399.1A patent/CN102190538B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4499327A (en) * | 1982-10-04 | 1985-02-12 | Union Carbide Corporation | Production of light olefins |
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101165018A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene |
| CN101348404A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for improving ethylene and propene yield in methyl alcohol or dimethyl ether conversion process |
| CN101318869A (en) * | 2008-06-12 | 2008-12-10 | 中国石油化工股份有限公司 | Process for converting oxygen-containing compound to prepare low carbon olefin hydrocarbon |
Non-Patent Citations (4)
| Title |
|---|
| 煤或天然气经甲醇制低碳烯烃工艺研究新进展;齐国祯等;《现代化工》;20050228;第25卷(第2期);第9-13页 * |
| 碳四烷烃催化裂解制低碳烯烃的研究进展;陆江银等;《现代化工》;20040831;第24卷(第8期);第15-18页 * |
| 陆江银等.碳四烷烃催化裂解制低碳烯烃的研究进展.《现代化工》.2004,第24卷(第8期),第15-18页. |
| 齐国祯等.煤或天然气经甲醇制低碳烯烃工艺研究新进展.《现代化工》.2005,第25卷(第2期),第9-13页. |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102190538A (en) | 2011-09-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101941875B (en) | Method for increasing production of low-carbon olefins | |
| CN101941876B (en) | Method for increasing production of light olefin | |
| CN102276386B (en) | Production method of light olefins | |
| CN102190548B (en) | Method for enhancing yield of light olefins in MTO technology | |
| CN102190542B (en) | The coupling process of methanol-to-olefins and carbon more than four hydrocarbon catalytic pyrolysis | |
| CN102295506B (en) | Method for producing low-carbon olefin by using methanol | |
| CN102276406B (en) | Method for increasing yield of propylene | |
| CN102464524B (en) | Method for producing low-carbon olefins from methanol | |
| CN102464523B (en) | Method for producing light olefins | |
| CN102190538B (en) | Method for Catalytic pyrolysis of hydrocarbons with more than 4 carbon atoms in process of preparing olefins from methanol | |
| CN102295507B (en) | Method for converting methanol or dimethyl ether into low-carbon olefin | |
| CN102190540B (en) | Method for producing propylene | |
| CN102276390A (en) | Method for adjusting product proportion in process of preparing olefin from methanol | |
| CN102464528B (en) | Method for increasing yields of ethylene and propylene | |
| CN102463079B (en) | Reaction device for producing low-carbon olefin from methanol | |
| CN103772089A (en) | Reaction device for improving yield of ethylene and propylene | |
| CN102295504B (en) | Method for preparing low-carbon olefin by using methanol | |
| CN103772088B (en) | Improve the method for ethene, propene yield | |
| CN102276395B (en) | Method for producing ethylene and propylene | |
| CN102190547B (en) | Improve the method for yield of light olefin products | |
| CN102464534B (en) | Method for producing low-carbon olefins from methanol | |
| CN102464527B (en) | Method for producing low-carbon olefins from low-carbon alcohols | |
| CN101293802A (en) | Method for preparing light olefin hydrocarbon with methanol or dimethyl ether | |
| CN102295501B (en) | Method for producing low-carbon olefin | |
| CN102276403B (en) | Method for producing low-carbon olefin |
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 |