CN103611581B - A kind of recovery of catalyst fines is used for the method for granulation again - Google Patents
A kind of recovery of catalyst fines is used for the method for granulation again Download PDFInfo
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- CN103611581B CN103611581B CN201310604158.5A CN201310604158A CN103611581B CN 103611581 B CN103611581 B CN 103611581B CN 201310604158 A CN201310604158 A CN 201310604158A CN 103611581 B CN103611581 B CN 103611581B
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- 239000003054 catalyst Substances 0.000 title claims abstract description 117
- 238000000034 method Methods 0.000 title claims abstract description 53
- 238000005469 granulation Methods 0.000 title claims abstract description 48
- 230000003179 granulation Effects 0.000 title claims abstract description 48
- 238000011084 recovery Methods 0.000 title claims abstract description 18
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims abstract description 63
- -1 alcohol ether alkene Chemical class 0.000 claims abstract description 47
- 230000008569 process Effects 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 239000002994 raw material Substances 0.000 claims abstract description 22
- 239000000428 dust Substances 0.000 claims abstract description 19
- 238000005243 fluidization Methods 0.000 claims abstract description 17
- 239000000843 powder Substances 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 27
- 239000000203 mixture Substances 0.000 claims description 24
- 230000000694 effects Effects 0.000 claims description 13
- 239000008367 deionised water Substances 0.000 claims description 12
- 229910021641 deionized water Inorganic materials 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 239000003546 flue gas Substances 0.000 claims description 8
- 238000005299 abrasion Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 239000012495 reaction gas Substances 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 7
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 6
- 238000010009 beating Methods 0.000 claims description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 6
- 238000007493 shaping process Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- 230000007423 decrease Effects 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 4
- 230000008439 repair process Effects 0.000 claims description 4
- 239000005995 Aluminium silicate Substances 0.000 claims description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 235000012211 aluminium silicate Nutrition 0.000 claims description 3
- 230000001186 cumulative effect Effects 0.000 claims description 3
- 229910001648 diaspore Inorganic materials 0.000 claims description 3
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 claims description 3
- 229910017604 nitric acid Inorganic materials 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 abstract description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 239000008187 granular material Substances 0.000 description 7
- 150000001336 alkenes Chemical class 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 230000005923 long-lasting effect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 241000700605 Viruses Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 208000030303 breathing problems Diseases 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002526 effect on cardiovascular system Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003979 granulating agent Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 230000036559 skin health Effects 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
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
-
- 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
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to the method for a kind of recovery of catalyst fines for granulation again, the method is applicable in alcohol ether alkene fluidized system, the method is collected by deduster in fluidized-bed reaction system from the catalyst fines in alcohol ether alkene fluidization system, the catalyst fines collected directly enters catalyst granulation process, and carry out mixing of arbitrary proportion with fresh catalyst raw material, thus instead of the raw material of part alcohol ether alkene catalyst granulation.In method of the present invention, alcohol ether alkene catalyst reclaims through deduster after wearing and tearing are broken into a large amount of fine powder, and the granulation process of catalyst for new lot, part granulating raw material is instead of when not affecting the alcohol ether alkene fluid catalyst performance indications of new granulation, thus play minimizing dust emission, reduce granulating raw material cost, save part expense expenditure environment amenable simultaneously.
Description
Technical field
The present invention relates to technical field of coal chemical industry, specifically, relate to the method for a kind of recovery of catalyst fines for granulation again.
Background technology
The abrasion strength resistance of catalyst is that can catalyst one of the key index realizing industrial applications.Owing to repeatedly flowing at reactor and regenerator Inner eycle in fluid bed inner catalyst long-time continuous, very violent friction is all there is between catalyst granules and catalyst granules, between catalyst granules and reactor wall and between catalyst and the air of flowing, therefore, catalyst in fluid bed is through long fluidisation, its abrasion strength resistance is in continuous decline, and final catalyst will be broken into granule and a large amount of fine powder.
In the past in the industrial production, a large amount of fine powders of generation were directly discharged in atmospheric environment, can cause dust pollution to environment, and dust pollution directly threatens the life of people, and the environment being especially in dust pollution can cause multiple cardiovascular, breathing problem etc.Dust pollution is for old man, the having the greatest impact of child, and too much dust easily grows germ virus to healthy totally unfavorable, also has great harm for skin health.
Now in the industrial production, in order to avoid dust pollution, the route of the comprehensive regulation will be walked, start with from production equipment, and select advanced reasonably plant equipment, be aided with certain dust-proof, dust suppression.But under the present conditions, most effective measures still select cleaner.The selection of cleaner will consider the aspects such as the character of degree of purification required by operation site and dust.For the collection of dust; the effective way of tradition adopts Pneumatic Dust Collecting Device or cloth bag dust collection equipment to collect the catalyst be worn then to carry out reprocessing; this mode makes the catalyst becoming fine powder can only be processed by as solid waste through process; dust polluting environment is avoided to have positive effect to protection of the environment; but equipment itself but adds operation cost and energy resource consumption, but do not create any economic benefit.
Summary of the invention
In order to solve catalyst recovery Problems existing in investment and energy resource consumption, the present invention proposes the method for a kind of recovery of catalyst fines for granulation again.
The method that the recovery of catalyst fines that the present invention develops is used for granulation again is mainly applicable in alcohol ether alkene fluidized system, the method is collected by deduster in fluidized-bed reaction system from the catalyst fines in alcohol ether alkene fluidization system, the catalyst fines collected just can directly enter catalyst granulation process without any alternate manner (such as acid modification or alkaline modification) process, and mixing of arbitrary proportion can be carried out with fresh catalyst raw material, thus instead of the raw material of part alcohol ether alkene catalyst granulation, part material in catalyst granulation process is recycled.
The method detailed process that recovery of catalyst fines of the present invention is used for granulation is again as follows:
(1) in reaction regeneration fluidized system, fill the catalyst with the alcohol ether alkene of certain tear strength; Be 300-750 DEG C in reaction temperature, pressure is that in the fluidisation system of 0.5-2.5MPa, alcohol ether alkene catalyst carries out circular response regenerative process;
(2) alcohol ether alkene catalyst contacts with alcohol ether in reactor, and catalysis alcohol ether is converted into olefin product.Long-lasting catalytic rubs with the gas of other catalyst granules, wall and flowing continuously.Along with the increase in reaction time, the tear strength of catalyst in continuous decline, thus causes catalyst abrasion to be broken into less particle and a large amount of fine powder.Wherein less particle (being greater than 5 microns) comes back to fluidisation system through the effect of cyclone and carries out reaction regeneration, and a large amount of fine powder (being less than 5 microns) can not by whirlwind effect along with process gas or flue gas be discharged from fluidisation system; Between reaction gas and the pipeline of flue gas, each increase dust arrester is for collecting the catalyst fines carried secretly in gas, also serves the effect of process for purifying gas and flue gas simultaneously;
(3) catalyst fines be collected into is As time goes on cumulative in the gathering-device of deduster, the granulation process of the catalyst being put in new lot is taken out artificially when running up to a certain amount of (being generally more than 5% of alcohol ether alkene catalyst quality), thus instead of the use of partially catalyzed agent granulating raw material, the restriction so both alleviating granulating raw material also suitably saves a part of raw material.While avoiding environment dust pollution, also save a part of financial cost.
Further, cyclone is preferably three grades of cyclones.Three grades of cyclones are considering for separating effect and economic factor.Be that progression is more in principle, separating effect is better.But three grades of whirlwind can isolate the fine powder of less than 5 microns, if add whirlwind again, separating effect can be better, but cost will raise a lot.If use secondary whirlwind or one cyclonic, just have a lot of granule and taken out of reaction-regeneration system, thus reduce the amount of the catalyst in reaction-regeneration system, affect reaction effect, and the use of more granulating agent can be increased.
Further, be 1-4.5m by the internal diameter of given reactor and regenerator, make superficial gas velocity in fluidization system between 1 ~ 9m/s, the too low alcohol ether alkene catalyst of gas speed and platinum group combustion adjuvant not energy fluidizing get up, thus the carrying out of impact reaction; The too high meeting of gas speed causes catalyst abrasion too serious, reduces the service life of catalyst.
Above-mentioned granulation process by the following method step carries out:
(1) deionized water and the solid Ludox contained for 30%-40% are 1.0-1.5:1.0 mix and blend 1.0h according to mass ratio;
(2) add solid containing the diaspore for 70%-80%, the ratio of itself and deionized water is 0.12-0.17:1.0, mix and blend 0.5-1.5h;
(3) add the alcohol ether alkene catalyst (the alcohol ether catalyst that part material or all raw material reclaim replaces) being milled to 0.1-5 micron, the ratio of itself and deionized water is 0.4-0.6:1.0, continuation mix and blend 1.0-1.5h;
(4) nitric acid adding appropriate 68% regulates PH=2.5-5.0, continues to stir 0.5-1.0h;
(5) add kaolin, the ratio of itself and deionized water is 0.4-0.6:1.0, mix and blend 1h;
(6) control beating pressure at 8.0-9.5MPa, vapo(u)rizing temperature 500-600 DEG C, outlet temperature is 200-250 DEG C, and making beating rotating speed is 1200-1500r/m, and shower nozzle adopts 1.0-2.0mm to carry out granulation;
(7) the shaping alcohol ether alkene catalyst after granulation is collected.
Due to the own particle diameter of alcohol ether alkene catalyst fine powder very little (being less than 5 microns) collected, simultaneously there is no to stick to each other between fine powder and fine powder and act on, without agglomerating clustering phenomena, present fluidized state.Therefore, while recovery uses catalyst fines, eliminate granulating raw material pulverize the processing steps such as grinding, to a certain extent, shorten the granulation process time, reduce job costs and labour intensity.
The average grain diameter of above-mentioned shaping alcohol ether alkene catalyst is at 50-100 micron, selective at 75%-85% to the gas phase of ethene and propylene, to the gas phase conversion rate of methyl alcohol more than 98%; Enhance abrasion strength resistance;
The repeatedly reaction regeneration that the method that recovery of catalyst fines of the present invention is used for granulation is again applicable to the catalyst fines in alcohol ether alkene fluidization system reclaims.
Innovation of the present invention and good effect are:
Recovery of catalyst fines of the present invention is used for the method for granulation again in alcohol ether alkene fluidized system, alcohol ether alkene catalyst reclaims through deduster after wearing and tearing are broken into a large amount of fine powder, and the granulation process of catalyst for new lot, part granulating raw material is instead of when not affecting the alcohol ether alkene fluid catalyst performance indications of new granulation, thus play minimizing dust emission, reduce granulating raw material cost, save part expense expenditure environment amenable simultaneously.
Accompanying drawing explanation
Fig. 1 is that the flow process of catalyst reaction regenerative process in alcohol ether alkene fluidization system involved in the present invention and catalyst fines collect schematic diagram.
Detailed description of the invention
Below in conjunction with accompanying drawing 1, the present invention is described further:
In alcohol ether alkene fluidized system, (see Fig. 1) realizes following technique:
(1) in reaction regeneration fluidized system, fill the catalyst with the alcohol ether alkene of certain tear strength, be 300-750 DEG C in reaction temperature, pressure is that in the fluidisation system of 0.5-2.5MPa, alcohol ether alkene catalyst carries out circular response regenerative process;
(2) alcohol ether alkene catalyst contacts with alcohol ether in reactor, and catalysis alcohol ether is converted into olefin product; Long-lasting catalytic rubs with the gas of other catalyst granules, wall and flowing continuously.Along with the increase in reaction time, the tear strength of catalyst in continuous decline, thus causes catalyst abrasion to be broken into less particle and a large amount of fine powder; Wherein less particle comes back to fluidisation system through the effect of three grades of cyclones and carries out reaction regeneration, and a large amount of fine powder can not by three grades of whirlwind effects along with process gas or flue gas be discharged from fluidisation system; Between reaction gas and the pipeline of flue gas, each increase dust arrester is for collecting the catalyst fines carried secretly in gas, also serves the effect of process for purifying gas and flue gas simultaneously;
(3) catalyst fines be collected into is As time goes on cumulative in the gathering-device of deduster, the granulation process of the catalyst being put in new lot is taken out artificially when running up to a certain amount of (being generally more than 5% of alcohol ether alkene catalyst quality), thus instead of the use of partially catalyzed agent granulating raw material, the restriction so both alleviating granulating raw material also suitably saves a part of raw material.While avoiding environment dust pollution, also save a part of financial cost.
Above-mentioned granulation process by the following method step carries out:
(1) deionized water and the solid Ludox contained for 30%-40% are 1.0-1.5:1.0 mix and blend 1.0h according to mass ratio
(2) add solid containing the diaspore for 70%-80%, the ratio of itself and deionized water is 0.12-0.17:1.0, mix and blend 0.5-1.5h;
(3) add the alcohol ether alkene catalyst (the alcohol ether catalyst that part material or all raw material reclaim replaces) being milled to 0.1-5 micron, the ratio of itself and deionized water is 0.4-0.6:1.0, continuation mix and blend 1.0-1.5h;
(4) nitric acid adding appropriate 68% regulates PH=2.5-5.0, continues to stir 0.5-1.0h;
(5) add kaolin, the ratio of itself and deionized water is 0.4-0.6:1.0, mix and blend 1h;
(6) control beating pressure at 8.0-9.5MPa, vapo(u)rizing temperature 500-600 DEG C, outlet temperature is 200-250 DEG C, and making beating rotating speed is 1200-1500r/m, and shower nozzle adopts 1.0-2.0mm to carry out granulation;
(7) the shaping alcohol ether alkene catalyst after granulation is collected.
Operating mode 1:
200-250g alcohol ether alkene catalyst is placed in fluidized reaction regenerative system, and wherein the internal diameter of reactor and regenerator is 120-300mm, reacts at the temperature of 300-450 DEG C, and the superficial gas velocity of catalyst is 1-9m/s.Device, through the operation of 10-15 days, receives the catalyst fines of 10-24g in deduster, and the catalyst fines collected is replaced granulation catalyst raw material, for the catalyst granulation process of new lot.Then the catalyst of new granulation is put into alcohol ether alkene fluid bed reaction-regeneration system to run, the olefin product obtained after operation and not contrasting with the olefin product of the method, data there is no significant change (see table 1, table 2).
| Product component | Gas phase selects (%) |
| Methane | 1.52 |
| Ethane | 0.40 |
| Ethene | 36.75 |
| Propane | 1.12 |
| Propylene | 41.14 |
| Gas phase conversion rate % | 98.90 |
Table 1 uses the catalyst fines granulation reaction gas phase selectivity reclaimed
| Product component | Gas phase selects (%) |
| Methane | 1.34 |
| Ethane | 0.51 |
| Ethene | 36.07 |
| Propane | 1.22 |
| Propylene | 41.00 |
| Gas phase conversion rate % | 98.76 |
Table 2 does not use the catalyst fines granulation reaction gas phase selectivity of recovery
Operating mode 2:
800-1000Kg alcohol ether alkene catalyst is placed in fluidized reaction regenerative system, and wherein the internal diameter of reactor and regenerator is 1.4-3.1m, reacts at the temperature of 400-450 DEG C, and the superficial gas velocity of catalyst is 1-9m/s.Device, through the operation of 100-120 days, receives the catalyst fines of 40-55Kg in deduster, and the catalyst fines collected is replaced granulation catalyst raw material, for the catalyst granulation process of new lot.Then the catalyst of new granulation is put into alcohol ether alkene fluid bed reaction-regeneration system to run, the olefin product obtained after operation and not contrasting with the olefin product of the method, data there is no significant change (see table 3, table 4).
| Product component | Gas phase selects (%) |
| Methane | 1.41 |
| Ethane | 0.38 |
| Ethene | 36.33 |
| Propane | 1.40 |
| Propylene | 43.26 |
| Gas phase conversion rate % | 99.77 |
Table 3 uses the catalyst fines granulation reaction gas phase selectivity reclaimed
| Product component | Gas phase selects (%) |
| Methane | 1.8 |
| Ethane | 0.58 |
| Ethene | 36.09 |
| Propane | 1.22 |
| Propylene | 42.03 |
| Gas phase conversion rate % | 99.74 |
Table 4 does not use the catalyst fines granulation reaction gas phase selectivity of recovery
Above one embodiment of the present of invention have been described in detail, but described content being only preferred embodiment of the present invention, can not being considered to for limiting practical range of the present invention.All equalizations done according to the present patent application scope change and improve, and all should still belong within patent covering scope of the present invention.
Claims (5)
1. a recovery of catalyst fines is used for the method for granulation again, it is characterized in that: the method is applicable in alcohol ether alkene fluidized system, the method is collected by deduster in fluidized-bed reaction system from the catalyst fines in alcohol ether alkene fluidization system, the catalyst fines collected directly enters catalyst granulation process, and carry out mixing of arbitrary proportion with fresh catalyst raw material, thus instead of the raw material of part alcohol ether alkene catalyst granulation; Described method detailed process is as follows:
(1) in alcohol ether alkene fluidized system, fill the catalyst with the alcohol ether alkene of tear strength; Be 300-750 DEG C in reaction temperature, pressure is that in the fluidisation system of 0.5-2.5MPa, alcohol ether alkene catalyst carries out circular response regenerative process;
(2) alcohol ether alkene catalyst contacts with alcohol ether in reactor, and along with the increase in reaction time, the tear strength of catalyst in continuous decline, thus causes catalyst abrasion to be broken into less particle and a large amount of fine powder; Wherein less particle comes back to fluidisation system through the effect of cyclone and carries out reaction regeneration, and a large amount of fine powder can not by whirlwind effect along with process gas or flue gas be discharged from fluidisation system; Between reaction gas and the pipeline of flue gas, each increase dust arrester is for collecting the catalyst fines carried secretly in gas;
(3) catalyst fines be collected into is As time goes on cumulative in the gathering-device of deduster, takes out the granulation process of the catalyst being put in new lot when running up to a certain amount of artificially;
Described a certain amount of be more than 5% of alcohol ether alkene catalyst quality;
Described cyclone is three grades of cyclones;
Reactor in described alcohol ether alkene fluidized system and the internal diameter of regenerator are 1-4.5m.
2. a kind of recovery of catalyst fines according to claim 1 is used for the method for granulation again, it is characterized in that: described granulation process by the following method step carries out:
(1) deionized water and the solid Ludox contained for 30%-40% are 1.0-1.5:1.0 mix and blend 1.0h according to mass ratio;
(2) add solid containing the diaspore for 70%-80%, the ratio of itself and deionized water is 0.12-0.17:1.0, mix and blend 0.5-1.5h;
(3) add the alcohol ether alkene catalyst being milled to 0.1-5 micron, wherein part material or alcohol ether catalyst that all raw material reclaims replace, and the ratio of itself and deionized water is 0.4-0.6:1.0, continuation mix and blend 1.0-1.5h;
(4) nitric acid adding appropriate 68% regulates pH=2.5-5.0, continues to stir 0.5-1.0h;
(5) add kaolin, the ratio of itself and deionized water is 0.4-0.6:1.0, mix and blend 1h;
(6) control beating pressure at 8.0-9.5MPa, vapo(u)rizing temperature 500-600 DEG C, outlet temperature is 200-250 DEG C, and making beating rotating speed is 1200-1500r/m, and shower nozzle adopts 1.0-2.0mm to carry out granulation;
(7) the shaping alcohol ether alkene catalyst after granulation is collected.
3. a kind of recovery of catalyst fines according to claim 2 is used for the method for granulation again, it is characterized in that: the average grain diameter of described shaping alcohol ether alkene catalyst is at 50-100 micron.
4. a kind of recovery of catalyst fines according to claim 2 is used for the method for granulation again, it is characterized in that: the gas phase of described shaping alcohol ether alkene catalyst to ethene and propylene is selective at 75%-85%, to the gas phase conversion rate of methyl alcohol more than 98%.
5. a kind of recovery of catalyst fines according to claim 1 is used for again the application of the method for granulation, it is characterized in that: the repeatedly reaction regeneration that described method is applicable to the catalyst fines in alcohol ether alkene fluidization system reclaims.
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| CN107442184B (en) * | 2016-06-01 | 2019-09-27 | 中国石化扬子石油化工有限公司 | A kind of recyclable device and recovery method of catalytic cracking catalyst fine powder |
| CN107971043A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The method and a kind of method of catalytic cracking catalyst production that a kind of beaded catalyst crushes |
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