CN103372460B - A kind of method utilizing the gaseous mixture regenerated methanol alkene catalyst of oxygen and carbon dioxide - Google Patents
A kind of method utilizing the gaseous mixture regenerated methanol alkene catalyst of oxygen and carbon dioxide Download PDFInfo
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- CN103372460B CN103372460B CN201210116232.4A CN201210116232A CN103372460B CN 103372460 B CN103372460 B CN 103372460B CN 201210116232 A CN201210116232 A CN 201210116232A CN 103372460 B CN103372460 B CN 103372460B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention provides a kind of renovation process of methanol-to-olefins used catalyst, mainly adopt the method for gaseous mixture as regeneration gas burn off catalyst carbon deposition of carbon dioxide and oxygen.By the volume ratio of regulation of carbon dioxide and oxygen, and regeneration temperature, the quantity that regenerated catalyst is residual with carbon distribution in duct on the surface can be controlled, and then control regenerated catalyst performance.This method dependable performance, flexible adjustment, running cost is low, and regenerative process is without NO
xproduce, environmental friendliness and the security of production operation can be improved.In addition, collection and the comprehensive utilization of carbon dioxide is also helped.
Description
Technical field
The present invention relates to a kind of method utilizing the gaseous mixture regenerated methanol alkene catalyst of oxygen and carbon dioxide.
Background technology
Along with the day by day exhaustion of fossil resources, be that the technique of raw material preparative chemistry product receives much concern with coal, wherein coal is also subject to extensive concern through the technique of methanol-to-olefins, and has obtained extraordinary economic benefit and social benefit.Industrial methanol-to-olefins adopts SAPO class catalyst, adopts fluidized-bed process process, and after reaction a period of time, in reactor, the catalyst of carbon distribution needs to carry out coke-burning regeneration, to recover the activity and selectivity of catalyst.In the prior art, the regenerative process of methanol-to-olefin catalyst adopts the gaseous mixture of nitrogen and air or water vapour and air as regeneration feed gas, by regulating the amount of nitrogen or water vapour in regeneration feed gas, prevent regenerative process from occurring " temperature runaway " or " tail combustion " phenomenon.But adopt in this way, high-temperature water vapor can cause catalyst activity component framework dealumination, and then destroy the stuctures and properties of catalyst; On the other hand, containing nitrogen in regeneration feed gas, in regenerative response process, NO can be produced
x, i.e. nitric oxide (NO) and nitrogen dioxide (NO
2) gaseous mixture, the NO of generation
xif be adsorbed on the surface of catalyst, and the regenerated catalyst be recycled brings reaction system into, this part NO
xlikely be brought into the separation of olefins workshop section in downstream.The operating temperature of separation of olefins workshop section is low, NO
xoccur abnormal accumulative, very easily cause the danger such as blast.In addition.NO in catalyst regeneration process
xemission problem also enjoy people to pay close attention to, NO
xbe not only the main component forming acid rain and photochemical fog, and be that regenerative system generation nitre is crisp, occur the main cause of crackle.So the present invention adopts carbon dioxide and oxygen to it also avoid NO as regeneration gas
xthe appearance of problem.Improve the security of production operation.
The regeneration techniques of molecular sieve industrial catalyst just develops rapidly along the Trinitarian direction of multi-series, high benefit, more environmental protection, not only recycle carbon dioxide with the gaseous mixture of carbon dioxide and oxygen as regeneration gas, but also be conducive to collection and the comprehensive utilization of carbon dioxide.This has just met the environmental protection policy of China.
Summary of the invention
The invention provides a kind of method utilizing the gaseous mixture regenerated methanol alkene catalyst of carbon dioxide and oxygen, adopt carbon dioxide and oxygen as regeneration gas, by the volume ratio of regulation of carbon dioxide and oxygen, and the temperature of regenerative operation, quantity residual with carbon distribution in duct on catalyst surface can be controlled, and then control regenerated catalyst performance.On the other hand, the present invention is also in order to avoid adopting water vapour and air to cross high catalyst to contact the framework dealumination phenomenon caused generation with water vapour as what produce during regeneration gas due to temperature, NO when employing nitrogen and oxygen also can be avoided to do regeneration gas regenerated methanol alkene catalyst
xthe generation of gas.
The invention provides a kind of method utilizing the gaseous mixture regenerated methanol alkene catalyst of carbon dioxide and oxygen, the method concrete steps are as follows:
(1) by the Catalyst packing of inactivation in methanol-to-olefins process in reactor, in reactor, pass into carbon dioxide purge 10 minutes.
(2) temperature of reactor heating furnace is set, when temperature rises to 200 DEG C, carbon dioxide is switched to the gaseous mixture of the carbon dioxide and oxygen of different volumes, start reaction of making charcoal, when temperature is raised to more than 450 DEG C, to make charcoal requirement according to difference, constant temperature some hours under regeneration temperature.Treat that temperature programming terminates stopping and making charcoal.
Described method, catalyst is methanol-to-olefin catalyst, and reaction system is methanol to olefins reaction, comprises the reaction of the olefin alkene such as Methanol ethene, propylene and fourth be rare, the reaction of preparing propylene from methanol, the reaction of Methanol ethene and propylene.
Carbon dioxide used can with replacing through deviating from the gaseous mixture after water vapour of producing in the regenerative process of methanol to olefins reaction system catalyst used, this gaseous mixture based on carbon dioxide, containing partial oxidation and carbon monoxide, wherein V (O
2)=(1%-15%), V (CO)=(10%-25%), all the other are carbon dioxide; Also can be the carbon dioxide after purifying, the carbon dioxide of purification can be the one in compression arbon dioxide, dry ice, liquid carbon dioxide.
In described step 3, regeneration gas volume ratio is V (CO
2): V (O
2): V (other gas)=(0%-80%): (10%-100%): (0%-10%).Preferred V (CO
2): V (O
2): V (CO)=(20%-50%): (40%-80%): (0%-10%).
Regeneration temperature in described step 3 is 450 DEG C-800 DEG C.Preferably 450 DEG C ~ 600 DEG C
The process regenerated in described method can regeneration in-situ regeneration or fluidized-bed reactor in in-situ regeneration.
Described do containing carbon dioxide and oxygen the carbon dioxide that regeneration gas comprises and also as the conveying gas of conveying catalyst and fluidized gas can be helped.
The invention has the advantages that the environmental protection and safety problem that not only solve and produce when doing regeneration gas with nitrogen and oxygen or water vapour and oxygen, but also create good condition for the recycling of carbon dioxide.Utilize the regeneration gas containing oxygen and carbon dioxide, the methanol-to-olefin catalyst of regeneration is evaluated via fixed bed evaluating apparatus, the olefine selective of catalyst and life-span all can recover, and repeatedly with the regeneration gas regenerated methanol alkene catalyst containing oxygen and carbon dioxide, the olefine selective of catalyst and life-span also can not decay.
Detailed description of the invention
Below by specific embodiment, the method utilizing oxygen and carbon dioxide gas mixture to do regeneration gas regenerated methanol alkene catalyst is further described, but the present invention is not therefore subject to any restriction.
Embodiment 1
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol mixed olefins, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to V (CO
2): V (O
2) be 80%: 20%, total flow is that the regeneration gas of 40mL/min carries out the reaction of burning carbon, when temperature is raised to 500 DEG C, constant temperature 3 hours.Treat that temperature programming terminates stopping and making charcoal, regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response, the conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 2
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol mixed olefins, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to V (CO
2): V (O
2) be 0%: 100%, total flow is that the regeneration gas of 20mL/min carries out the reaction of burning carbon, when temperature is raised to 800 DEG C, constant temperature two hours.Treat that temperature programming terminates stopping and making charcoal, regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response, the conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 3
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol mixed olefins, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to liquid carbon dioxide, V (CO
2): V (O
2) be 66%: 34% regeneration gas carry out burning carbon reaction, when temperature is raised to 650 DEG C, constant temperature 2 hours.Treat that temperature programming terminates stopping and making charcoal.Again regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response, the conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 4
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol ethene and propylene, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to CO
2: CO: O
2volume ratio be 40%: 20%: 40% regeneration gas carry out burning carbon reaction, when temperature is raised to 650 DEG C, constant temperature two hours.Treat that temperature programming terminates stopping and making charcoal.Again regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into methyl alcohol, start the evaluation response of Methanol ethene and propylene.After temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response, the conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 5
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol ethene and propylene, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to compression arbon dioxide, compression arbon dioxide is converted to standard state V (CO
2): V (O
2) be 70%: 30% regeneration gas carry out burning carbon reaction, when temperature is raised to 650 DEG C, constant temperature two hours.Treat that temperature programming terminates stopping and making charcoal.Again regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response.The conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 6
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol mixed olefins, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to and stores up tank connected pipeline with dry ice, V (the CO when carbon dioxide produced after dry ice is heated is converted to standard state
2): V (O
2) be 66%: 34% regeneration gas carry out burning carbon reaction, when temperature is raised to 650 DEG C, constant temperature two hours.Treat that temperature programming terminates stopping and making charcoal.Again regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response.The conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 7
4g methanol-to-olefin catalyst (imvite: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) is loaded in reactor, carry out the reaction of Methanol mixed olefins, the methanol aqueous solution of reaction raw materials to be concentration be 40wt%, reaction temperature is 450 DEG C, pressure is 0.005MPa, and air speed is 1.5h
-1.After reaction inactivation, in reactor, pass into the carbon dioxide purging that flow is 40mL/min, reactor furnace temp is set; When temperature rises to 200 DEG C, the emission gases through dust removal process (about containing CO2 content is 80%) produced when carbon dioxide being switched to regenerated methanol alkene catalyst, by adding oxygen, makes V (CO
2): V (O
2) be 80%: 20% gaseous mixture carry out burning carbon reaction, when temperature is raised to 650 DEG C, constant temperature two hours.Treat that temperature programming terminates stopping and making charcoal.Again regeneration gas is switched to carbon dioxide, keep 20min when furnace temp is down to 450 DEG C, after temperature stabilization, pass into the methanol aqueous solution that concentration is 40wt%, air speed is 1.5h
-1, pressure is that 0.005MPa starts Methanol mixed olefins evaluation response.The conversion of olefines rate of regenerated catalyst and selective in table 1.
Embodiment 8
The catalyst (kaolin: Alumina gel: SAPO-34 molecular sieve=30wt%: 31wt%: 39wt%) of 4g methanol-to-olefins inactivation is loaded in regenerator, in regenerator, pass into the carbon dioxide purging that flow is 40mL/min, regenerator furnace temp is set; When temperature rises to 200 DEG C, carbon dioxide is switched to the gaseous mixture of carbon dioxide and oxygen, use V (CO
2): V (O
2) be 80%: 20% gaseous mixture carry out burning carbon reaction, when temperature is raised to 700 DEG C, constant temperature four hours.Catalyst after regeneration is loaded in preparing propylene from methanol reactor and reacts.The concentration of the material benzenemethanol aqueous solution is 40wt%, and reaction temperature is 415 DEG C, and reaction pressure is 0.13MPa, and air speed is 1.5h
-1.Olefine selective and life-span are in table 1.
Table 1
Remarks:
*: " fresh catalyst " refers in embodiment 1 catalyst (namely mixing the catalyst of alkene first for Methanol) not having used Methanol to mix alkene.
Claims (7)
1. utilize a method for the gaseous mixture regenerated methanol alkene catalyst of carbon dioxide and oxygen, concrete steps are as follows:
(1) by the Catalyst packing of inactivation in methanol-to-olefins process in reactor, in reactor, pass into carbon dioxide, purge 10 minutes;
(2) temperature of reactor heating furnace is set, when the temperature in question response device rises to 200 DEG C from room temperature, carbon dioxide is switched to V (CO
2): V (O
2): V (CO)=(0%-80%): (10%-100%): the gaseous mixture based on carbon dioxide and oxygen of (0%-10%), start reaction of making charcoal, when temperature rises to 450 DEG C-800 DEG C, to make charcoal requirement according to difference, constant temperature 1-10 hour under regeneration temperature.
2. method according to claim 1, is characterized in that: described catalyst is methanol-to-olefins class reaction system catalyst used; Described reaction system is methanol to olefins reaction, the reaction of the rare mixed olefins of Methanol ethene, propylene and fourth, the reaction of preparing propylene from methanol, or the reaction of Methanol ethene and propylene.
3. method according to claim 1 and 2, is characterized in that: described catalyst mainly consists of the clay based on Silicified breccias: aluminium source: SAPO-34 molecular sieve=(30wt%-65wt%): (0.5wt%-31wt%): (19wt%-42wt%).
4. method according to claim 1, it is characterized in that: the gaseous mixture after deviating from water vapour produced in the regenerative process of the catalyst that carbon dioxide methanol to olefins reaction system used is used replaces, this gaseous mixture is based on carbon dioxide, containing partial oxidation and carbon monoxide, wherein V (O
2)=(1%-15%), V (CO)=(10%-25%), all the other are carbon dioxide; Or the carbon dioxide after purifying, the carbon dioxide of purification is the one in compression arbon dioxide, dry ice, liquid carbon dioxide.
5. according to the method described in claim 1, it is characterized in that: V (CO
2): V (O
2): V (CO)=(20%-50%): (40%-80%): (0%-10%).
6. according to the method described in claim 1, it is characterized in that: the temperature of regeneration is 450 DEG C ~ 650 DEG C.
7. according to the method described in claim 1, it is characterized in that: described reactor is regenerator or fluidized-bed reactor, process in-situ regeneration in regeneration in-situ regeneration or fluidized-bed reactor of regeneration.
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| CN110878002B (en) * | 2018-09-06 | 2022-11-22 | 中国科学院大连化学物理研究所 | Method for regenerating carbon deposition catalyst and co-producing carbon dioxide |
| CN115055211A (en) * | 2022-06-10 | 2022-09-16 | 中国石油大学(北京) | Methanol-to-olefin regeneration method with carbon dioxide zero emission and carbon monoxide byproduct |
| CN115055212A (en) * | 2022-06-10 | 2022-09-16 | 中国石油大学(北京) | Regeneration method for preparing olefin from methanol with zero emission of carbon dioxide |
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| US20050043577A1 (en) * | 2003-08-22 | 2005-02-24 | Beech James Harding | Catalyst regenerator for reducing entrained catalyst loss and processes for using same |
| CN101279872A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin hydrocarbon with oxocompound |
| CN101327445A (en) * | 2008-06-12 | 2008-12-24 | 中国石油化工股份有限公司 | High-efficient regeneration method for preparing light olefins catalyst from oxygen-containing compounds |
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| US20050043577A1 (en) * | 2003-08-22 | 2005-02-24 | Beech James Harding | Catalyst regenerator for reducing entrained catalyst loss and processes for using same |
| CN101279872A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin hydrocarbon with oxocompound |
| CN101327445A (en) * | 2008-06-12 | 2008-12-24 | 中国石油化工股份有限公司 | High-efficient regeneration method for preparing light olefins catalyst from oxygen-containing compounds |
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Commission number: 4W111575 Conclusion of examination: On the basis of claims 1-6 modified by the patentee on March 12, 2021, the validity of invention patent right No. 201210116232.4 is maintained Decision date of declaring invalidation: 20210820 Decision number of declaring invalidation: 51398 Denomination of invention: A Method for Regenerating Methanol to Olefin Catalysts Using a Mixture of Oxygen and Carbon Dioxide Granted publication date: 20150930 Patentee: CHIA TAI ENERGY MATERIALS (DALIAN) Co.,Ltd. |