CN105080592A - Aromatic olefin-reducing catalyst and use thereof - Google Patents
Aromatic olefin-reducing catalyst and use thereof Download PDFInfo
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Abstract
The present invention relates to an aromatic olefin-reducing catalyst mainly solving the problems of short carclazyte life, frequent replacement, large labor intensity, and serious environmental pollution when the carclazyte is used for removing trace olefins in an aromatic material in current industry. The aromatic olefin-reducing catalyst is used, the average pore diameter of the aromatic olefin-reducing catalyst is 5-30nm, the aromatic olefin-reducing catalyst comprises the following components by weight: 0 to 15% of lanthanide elements or a mixture thereof; 0 to 20% of oxides of one or more elements selected from Ca, Zn , Mg and Ti; and 30 to 90% of a molecular sieve, the molecular sieve is at least one selected from mordenite, Y zeolite, ZSM-5 molecular sieve, MCM-22 molecular sieve, MCM-56 molecular sieve, and beta-molecular sieve; and a carrier is one substance selected from alumina and silica or a mixture thereof, and by the technical scheme, the problem is preferably solved, and the method can be used for aromatic olefin-reducing industrial production.
Description
Technical field
The present invention relates to a kind of olefin-reducing catalyst for aromatic hydrocarbons, may be used for alternative industrial carclazyte, it is short to solve its life-span, and change frequent, labour intensity is large, the problem that environmental pollution is serious.
Technical background
Aromatic hydrocarbons is the base stock of petrochemical industry, and it mainly comes from Aromatic Hydrocarbon United Plant.Aromatic hydrocarbon product after catalytic reforming reaction is all containing a certain amount of olefin impurity.Alkene character is enlivened, and not only easily polymerization forms colloid, but also may react with other component, generates undesirable components, thus produces considerable influence to the quality of aromatic hydrocarbon product.
On the other hand, some petrochemical process process is as responsive especially to alkene in dimethylbenzene adsorption separation process, even if the content of olefin impurity only has a few millionths, also can produce very adverse influence to technical process.In order to obtain qualified industrial chemicals and ensure carrying out smoothly of subsequent technique, after reformation, Aromatics Extractive Project, isomerization, toluene disproportionation operation, all there is refining step to remove trace amounts of olefin impurity.
Because refining steps all in current Aromatic Hydrocarbon United Plant all adopts carclazyte as finishing agent, along with the popularization that low pressure is reformed, in reformate, gum level increases, and the puzzlement that carclazyte brings will be more serious, in the urgent need to substituting efficient olefinic hydrocarbon expelling catalyzer and the application technology of industrial carclazyte.
Carclazyte has acid centre, under high pressure liquid phase, 150 ~ 200 DEG C of conditions, there is certain catalytic polymerization ability and duct adsorption capacity, the reaction such as trace amounts of olefin generation hydrocarbonylation, polymerization contained in reformate can be made, generate higher-boiling compound, then by bleaching earth adsorption, or remove in later separation flow process.
The alkene in reformate is removed with clay-filtered route, good effect is had to removing alkene in the long distillate from benzene to dimethylbenzene, but because carclazyte activity is low, life-span is short, need frequent replacing, thus causing the use amount of carclazyte very large, labour intensity is also large, constrains device " long surely excellent " operation.
Exploitation carclazyte can cause the permanent damage of environment.In addition, after inactivation containing aromatic hydrocarbons carclazyte due to very unfavorable to health, cannot recycle, can only be processed by landfill, this just causes serious secondary pollution to environment.In today that environmental consciousness is constantly strengthened, this problem more and more receives the concern of country and the common people, the catalysis deolefination technology of manufacturing enterprise in the urgent need to addressing these problems.
Chinese patent CN1618932 describes one catalytic refining reforming aromatic oil catalyst under conditions of non-hydrogen.This catalyst is non-loading type solid acid catalyst, adopts this catalyst treatment reforming aromatic oil, and reaction temperature 100 ~ 300 DEG C, reaction pressure 0.5 ~ 3.0MPa, when air speed 0.5 ~ 40
-1under condition, can trace amounts of olefin in Arene removal, although but this catalyst can regenerate and reuse, its single pass life is still too short, when air speed is 15
-1after checking and rating 18 hours under condition, its activity is just reduced to 50%, and thus commercial Application is very limited.
Adopting olefinic hydrocarbon expelling catalyzer to substitute industrial carclazyte is a new research field, and achievement in research is in this respect few at present, and acquired technological achievement is limited, and the catalyst activity of exploitation is low, the life-span is short, and aromatic hydrocarbons loss is large, does not also possess industrial application value.
Summary of the invention
One of technical problem to be solved by this invention is short for the carclazyte life-span in clay-filtered deolefination method, and change frequent, labour intensity is large, the problem that environmental pollution is serious, provide a kind of novel olefin-reducing catalyst for aromatic hydrocarbons, there is carbon accumulation resisting ability strong, good stability, aromatic hydrocarbons loses few feature, single pass life can reach more than 10 times of carclazyte, reaches more than 50 times of carclazyte entire life, effectively reduces labour intensity, alleviate environmental pollution, prospects for commercial application is good.
Two of technical problem to be solved by this invention is to provide a kind of purposes of the catalyst corresponding with one of technical solution problem.
For one of solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of olefin-reducing catalyst for aromatic hydrocarbons, by weight percentage, comprises following component:
A) 0.05 ~ 15% lanthanide series or its mixture;
B) 0.05 ~ 20% oxide being selected from one or more elements in Ca, Zn, Mg, Ti, P;
C) molecular sieve of 30 ~ 90%, molecular screening from modenite, Y zeolite, ZSM-5 molecular sieve, MCM-22 molecular sieve, MCM-56 molecular sieve, at least one in beta-molecular sieve;
D) surplus is be selected from aluminium oxide, the one of silica or its mixture.
In technique scheme, the described olefin-reducing catalyst for aromatic hydrocarbons average pore size of mesoporous solid acid catalyst is 5 ~ 30nm, and specific area is 350 ~ 800cm2/g, and pore volume is 0.35 ~ 1.0cm3/g; Average pore size preferable range is 8-20nm, and specific area preferable range is 450 ~ 700cm2/g, and pore volume preferable range is 0.38 ~ 0.85cm3/g; The pore volume that the duct that aperture is greater than 10nm provides accounts for more than 60% of total pore volume; By weight percentage, the preferable range of lanthanide series or its mixture content is 0.1 ~ 12%; The preferable range being selected from the oxide content of one or more elements in Ca, Zn, Mg, Ti, P, Sn, Fe is 0.3-15%; One or more are selected from modenite, Y zeolite, ZSM-5 molecular sieve, MCM-22 molecular sieve, MCM-56 molecular sieve, and the preferable range of the molecular sieve content in UZM-8, beta-molecular sieve is 50-85%; In molecular sieve, Na, K or its mixture are less than 2.0% by weight percentage.
For solve the problems of the technologies described above two, the technical solution used in the present invention is as follows: be 80 ~ 300 DEG C in reaction temperature, and reaction pressure is 0.5 ~ 3.0MPa, weight space velocity 0.3 ~ 10h
-1condition under, the aroamtic hydrocarbon raw material containing alkene is contacted with said mesoporous solid acid catalyst, makes the alkene in raw material change higher boiling product into, and remove in subsequent separation process; Said mesoporous solid acid catalyst is used for Olefin decrease reaction, and its single pass life can reach more than 4000 hours.
The present invention take molecular sieve as active main body, after mixing with binding agent and modified additive and pore-creating auxiliary agent, through kneading, extrusion, dry, roasting, obtained finished catalyst after pelletizing.The acidity of auxiliary agent to catalyst that the present invention adopts has promotor action, improve the carbon accumulation resisting ability of catalyst, pore-creating auxiliary agent used forms space network in forming process simultaneously, then remove in roasting process, thus generation has larger-diameter pore passage structure, is conducive to the diffusion of reaction raw materials and product, reduces carbon deposition rate, extend catalyst life, thus obtain good technique effect.
The olefin-reducing catalyst for aromatic hydrocarbons that the present invention relates to is applicable to the Olefin decrease subtractive process of reformed oil in olefin(e) centent lower aromatic hydrocarbons material, particularly Aromatic Hydrocarbon United Plant, directly can substitute industrial carclazyte when not transforming existing apparatus.Use catalyst of the present invention, reaction temperature 170 DEG C, pressure 2.0PMa, mass space velocity 3.0h
-1condition under, catalyst initial activity can reach 98%, and the life-span, single pass life can reach more than 10 times of the carclazyte life-span under identical operating mode more than 4000 hours, more than 50 times of entire life.
Below by the description to embodiment, further illustrate but do not limit the present invention.
Embodiment
[embodiment 1]
Get Na
2o content is less than the boehmite (α-Al of 0.15% (weight), 550 DEG C of calcination losses 30%
2o
3h
2o) 128.57 grams, with Na
2o content is less than 1.5% (weight), the modenite 11.10 grams of calcination loss 10% mixes, with 2.5 milliliters, chemical pure nitric acid and 65 ml water wiring solution-formings.This mixed solution is added in the mixture of boehmite and modenite, mix, mediate extruded moulding, in 550 DEG C of roastings 3 hours after drying, obtained aluminium oxide: the catalyst A-1 of molecular sieve=90:10.
[embodiment 2 ~ 3]
Adopt the preparation method of embodiment 1, the ratio of adjustment molecular sieve and boehmite, respectively obtained aluminium oxide: the catalyst A-2 of molecular sieve=50:50 and aluminium oxide: the catalyst A-3 of molecular sieve=10:90.
[embodiment 4 ~ 10]
Modenite used for A-2 is changed respectively into β zeolite, X zeolite, Y zeolite, ZSM-5 molecular sieve, SAPO-11 molecular sieve, MCM-41 molecular sieve, TS molecular sieve, in kind obtain B, C, D, E, F, G, H catalyst respectively.
[embodiment 11]
Get Na
2o content is less than the boehmite (α-Al of 0.15% (weight), 550 DEG C of calcination losses 30%
2o
3h
2o) 42.86 grams, with Na
2o content is less than 1.5% (weight), the modenite 38.89 grams of calcination loss 10%, 38.89 grams, Y zeolite mix, with 2.5 milliliters, chemical pure nitric acid and 65 ml water wiring solution-formings.This mixed solution is added in the mixture of boehmite and molecular sieve, mix, mediate extruded moulding, in 550 DEG C of roastings 3 hours after drying, obtained aluminium oxide: modenite: the catalyst I of Y zeolite=30:35:35.
[embodiment 12 ~ 13]
Adopt the preparation method of embodiment 11, the ratio of adjustment molecular sieve and boehmite, respectively obtained aluminium oxide: SAPO-11 zeolite: the catalyst J of β zeolite=30:35:35 and aluminium oxide: ZSM-5 molecular sieve: β zeolite: the catalyst K of Y zeolite=30:23:23:24.
[embodiment 14]
In fixed bed reactors, carried out the test of reformate non-hydrogen deolefination with catalyst A ~ K obtained in embodiment 1 ~ 13, raw material is reformate, and bromine index is 650 milligrams of Br/100 gram of oil.Reaction pressure: 2.0MPa, temperature: 160 DEG C, air speed: when 10.0
-1, the results are shown in Table 1 (aromatic hydrocarbons loss refer to reaction after two hours sample analysis result).
[embodiment 15]
Get Na
2o content is less than the boehmite (α-Al of 0.15% (weight), 550 DEG C of calcination losses 30%
2o
3h
2o) 71.43 grams, with Na
2o content is less than 1.5% (weight), the modenite 55.56 grams of calcination loss 10% mixes, with chemical pure nickel nitrate 2.48 grams, 0.46 gram, chemical pure sulfuric acid, 2.5 milliliters, chemical pure nitric acid and 65 ml water wiring solution-formings.This mixed solution is added in the mixture of boehmite and modenite, mix, mediate extruded moulding, in 550 DEG C of roastings 3 hours after drying, obtained catalyst K-1.
[embodiment 16 ~ 38]
Adopt solution powder in embodiment 15 to mediate method, change solution composition, respectively catalyst K-2 ~ 24 of obtained different additive modification.
[embodiment 39]
Get Na
2o content is less than 0.15% (weight), SiO
2the Ludox of content 40% 75 grams, with Na
2o content is less than 1.5% (weight), the modenite 77.78 grams of calcination loss 10% mixes, with chemical pure nickel nitrate 2.48 grams, 0.46 gram, chemical pure sulfuric acid, 22.5 ml water wiring solution-formings.This mixed solution is added in the mixture of Ludox and modenite, mix, mediate extruded moulding, in 550 DEG C of roastings 3 hours after drying, obtained catalyst L-1.
[embodiment 40]
Get Na
2o content is less than 0.15% (weight), SiO
2the Ludox of content 40% 50 grams, Na
2o content is less than the boehmite (α-Al of 0.15% (weight), 550 DEG C of calcination losses 30%
2o
3h
2o) 28.57 grams, with Na
2o content is less than 1.5% (weight), the modenite 66.67 grams of calcination loss 10% mixes, with chemical pure nickel nitrate 2.48 grams, 0.46 gram, chemical pure sulfuric acid, 1.5 milliliters, chemical pure nitric acid and 36 ml water wiring solution-formings.This mixed solution is added in powder, mixes, mediate extruded moulding, in 550 DEG C of roastings 3 hours after drying, obtained catalyst L-2.
[comparative example 1]
When not doing any modification, be that catalyst carries out performance with the catalyst of invention and contrasts with atlapulgite, atlapulgite is numbered P.
[embodiment 41]
With catalyst K-1 ~ 24 obtained in embodiment 15 ~ 38, in fixed bed reactors, carried out the test of reformate non-hydrogen deolefination, raw material is reformate, and bromine index is 650 milligrams of Br/100 gram of oil.Reaction pressure: 2.0MPa, temperature: 160 DEG C, air speed: when 10.0
-1, the results are shown in Table 2 (aromatic hydrocarbons loss refer to reaction after two hours sample analysis result).
As can be seen from Table 2, the stability of metal promoter to catalyst is significantly improved, but amount of auxiliary too high meeting covering catalyst activated centre, or blocking catalyst duct, cause stability to reduce.
[embodiment 42]
By the catalyst P in catalyst L-1 ~ 2 obtained in embodiment 39 ~ 40 and comparative example 1, in fixed bed reactors, carried out the test of reformate non-hydrogen deolefination, raw material is reformate, and bromine index is 650 milligrams of Br/100 gram of oil.Reaction pressure: 2.0MPa, temperature: 160 DEG C, air speed: when 10.0
-1, the results are shown in Table 3 (aromatic hydrocarbons loss refer to reaction after two hours sample analysis result).
Table 3
| Catalyst | L-1 | L-2 | P |
| 2 hours initial activities | 91.53 | 92.76 | 90.38 |
| 100 hours active | 90.66 | 90.37 | 79.55 |
| 200 hours active | 88.74 | 87.16 | 51.24 |
| Aromatic hydrocarbons loses, % | 0.25 | 0.34 | 0.58 |
[embodiment 43]
With catalyst K-1 described in embodiment 15, fixed bed reactors have carried out the stability test of reformate deolefination, temperature 170 DEG C, pressure 2.0MPa, raw material bromine index is 650 milligrams of Br/100 gram of oil, during weight space velocity 3.0
-1, the results are shown in Table 4.
Table 4
| The duration of runs, time | Activity, % | Aromatic hydrocarbons loses |
| 2 hours | 97.58 | 0.35 |
| 100 hours | 97.26 | 0.30 |
| 200 hours | 97.31 | 0.30 |
| 300 hours | 96.75 | 0.27 |
| 500 hours | 95.90 | 0.21 |
| 1000 hours | 94.88 | 0.23 |
| 1500 hours | 92.16 | 0.19 |
| 2000 hours | 90.42 | 0.15 |
| 3000 hours | 87.90 | 0.18 |
[embodiment 44]
To checking and rating the catalyst K-1 after 3000 hours described in embodiment 43, carrying out coke-burning regeneration, then on fixed bed reactors, having carried out the stability test of reformate deolefination, temperature 170 DEG C, pressure 2.0MPa, raw material bromine index is 650 milligrams of Br/100 gram of oil, during weight space velocity 3.0
-1, the results are shown in Table 4.
Table 5
| The duration of runs, time | Activity, % | Aromatic hydrocarbons loses |
| 2 hours | 97.39 | 0.30 |
| 100 hours | 97.52 | 0.27 |
| 200 hours | 97.14 | 0.30 |
| 300 hours | 96.54 | 0.31 |
| 500 hours | 95.78 | 0.27 |
| 1000 hours | 94.26 | 0.19 |
| 1500 hours | 92.44 | 0.22 |
| 2000 hours | 89.85 | 0.18 |
| 3000 hours | 87.83 | 0.20 |
From table 5, after the regeneration of this new catalyst, performance is recovered substantially completely, illustrates that it has good regenerability, thus greatly extends its industrial application life-span.
Claims (10)
1. an olefin-reducing catalyst for aromatic hydrocarbons, in catalyst weight percent, comprises following component:
A) 0.05 ~ 15% lanthanide series or its mixture;
B) 0.05 ~ 20% be selected from least one element in Ca, Zn, Mg, Ti, P or its oxide;
C) molecular sieve of 30 ~ 90%, described molecular screening from modenite, Y zeolite, ZSM-5 molecular sieve, MCM-22 molecular sieve, MCM-56 molecular sieve, at least one in beta-molecular sieve;
D) at least one being selected from aluminium oxide or silica of 5 ~ 65%.
2. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, it is characterized in that described olefin-reducing catalyst for aromatic hydrocarbons average pore size is 5 ~ 30nm, specific area is 350 ~ 800cm
2/ g, pore volume is 0.35 ~ 1.0cm
3/ g.
3. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, it is characterized in that the average pore size of described catalyst is 8-20nm, specific area is 450 ~ 700cm
2/ g, pore volume is 0.38 ~ 0.85cm
3/ g.
4. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, is characterized in that the pore volume that the duct that said mesoporous solid acid catalyst mesoporous is greater than 10nm provides accounts for more than 60% of total pore volume.
5. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, is characterized in that said mesoporous solid acid catalyst by weight percentage, containing 0.1 ~ 12% lanthanide series or its mixture.
6. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, is characterized in that said mesoporous solid acid catalyst by weight percentage, is selected from the oxide of one or more elements in Ca, Zn, Mg, Ti, P, Sn, Fe containing 0.3-15%.
7. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, it is characterized in that said mesoporous solid acid catalyst by weight, molecular sieve containing 50-85%, molecular screening from modenite, Y zeolite, ZSM-5 molecular sieve, MCM-22 molecular sieve, MCM-56 molecular sieve, one or more in UZM-8, beta-molecular sieve.
8. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, is characterized in that in the molecular sieve that said mesoporous solid acid catalyst contains, Na, K or its mixture are less than 2.0% by weight percentage.
9. olefin-reducing catalyst for aromatic hydrocarbons according to claim 1, it is characterized in that said mesoporous solid acid catalyst can be 80 ~ 300 DEG C in reaction temperature, reaction pressure is 0.5 ~ 3.0MPa, weight space velocity 0.3 ~ 10h
-1condition under, make to generate higher boiling product containing the alkene in the aroamtic hydrocarbon raw material of alkene, and remove in subsequent separation process.
10. olefin-reducing catalyst for aromatic hydrocarbons according to claim 9, it is characterized in that said mesoporous solid acid catalyst reacts for Olefin decrease, catalyst initial activity can reach 98%, and single pass life can reach more than 4000 hours.
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| CN106563495A (en) * | 2016-10-31 | 2017-04-19 | 华南理工大学 | Glucose isomerization molecular sieve catalyst and preparation method thereof |
| WO2017197515A1 (en) * | 2016-05-16 | 2017-11-23 | Meg Energy Corp. | Direct olefin reduction of thermally cracked hydrocarbon streams |
| CN107754845A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | High life reformate olefine lowering catalyst |
| CN107754846A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation |
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| WO2017197515A1 (en) * | 2016-05-16 | 2017-11-23 | Meg Energy Corp. | Direct olefin reduction of thermally cracked hydrocarbon streams |
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| CN107754845A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | High life reformate olefine lowering catalyst |
| CN107754846A (en) * | 2016-08-23 | 2018-03-06 | 中国石油化工股份有限公司 | The reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation |
| CN107754846B (en) * | 2016-08-23 | 2019-11-08 | 中国石油化工股份有限公司 | The reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation |
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| CN106563495A (en) * | 2016-10-31 | 2017-04-19 | 华南理工大学 | Glucose isomerization molecular sieve catalyst and preparation method thereof |
| CN109351366A (en) * | 2018-10-16 | 2019-02-19 | 江苏华伦化工有限公司 | The method for reducing high boiling aromatic hydrocarbon solvent bromine index |
| CN109433250A (en) * | 2018-10-16 | 2019-03-08 | 江苏华伦化工有限公司 | Reduce the catalyst of high boiling aromatic hydrocarbon solvent bromine index |
| CN112657535B (en) * | 2019-10-16 | 2023-01-24 | 中国石油化工股份有限公司 | Olefin removal catalyst, and preparation method and application thereof |
| CN112657535A (en) * | 2019-10-16 | 2021-04-16 | 中国石油化工股份有限公司 | Olefin removal catalyst and preparation method and application thereof |
| CN110813370A (en) * | 2019-10-29 | 2020-02-21 | 浙江工业大学 | Method for refining aromatic hydrocarbon by utilizing microporous mesoporous core-shell structure composite molecular sieve |
| CN110813370B (en) * | 2019-10-29 | 2022-05-24 | 浙江工业大学 | Method for refining aromatic hydrocarbon by utilizing microporous mesoporous core-shell structure composite molecular sieve |
| CN114471704A (en) * | 2020-10-23 | 2022-05-13 | 华东理工大学 | Preparation of montmorillonite nanosheet loaded trifluoromethanesulfonic acid material and application of montmorillonite nanosheet loaded trifluoromethanesulfonic acid material in removal of trace olefins in aromatic hydrocarbons |
| WO2023061435A1 (en) * | 2021-10-13 | 2023-04-20 | 中国石油化工股份有限公司 | Olefin conversion catalyst, preparation method therefor and application thereof |
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Application publication date: 20151125 |