CN104437595A - Methanol-to-arene fluidized bed catalyst and preparation method thereof - Google Patents
Methanol-to-arene fluidized bed catalyst and preparation method thereof Download PDFInfo
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- CN104437595A CN104437595A CN201310435120.XA CN201310435120A CN104437595A CN 104437595 A CN104437595 A CN 104437595A CN 201310435120 A CN201310435120 A CN 201310435120A CN 104437595 A CN104437595 A CN 104437595A
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Abstract
The invention relates to a methanol-to-arene fluidized bed catalyst containing Zn and a preparation method thereof. The methanol-to-arene fluidized bed catalyst is mainly used for solving the technical problem that the existing methanol-to-arene fluidized bed catalyst containing Zn has Zn loss in calcinations and hydro-thermal treatment processes. In order to better solve the problem, the technical scheme adopted by the invention is as follows: the methanol-to-arene fluidized bed catalyst provided by the invention comprises the following components in percentage by weight: 1) 10.-40.0% of adhesive; 2) 20.0-55.0% of aluminosilicate substrate; 3) 20.0-70.0% of HZSM-5 molecular sieve; 4) 0.1-10% of ZnO, wherein the adhesive is selected from silicon-containing species. The methanol-to-arene fluidized bed catalyst containing Zn can be used in the industrial production of methanol-to-arene.
Description
Technical field
The present invention relates to a kind of Methanol aromatic hydrocarbons fluid catalyst containing Zn and preparation method thereof.
Background technology
Based on Organic Chemicals, the aromatic hydrocarbons of China more than 85% is all produced by petroleum path.On the one hand, China's oil and natural gas resource are very short, cause the production cost of aromatic hydrocarbons day by day to rise; On the other hand, coal resources in China relative abundance, the production capacity of a large amount of coal-based methanol finds new outlets.Therefore, Methanol aromatic hydrocarbons is a very promising technology path.
Methanol aromatic hydrocarbons is a typical acid catalyzed reaction, and catalyst used is normally obtained on acidic molecular sieve by metal (Ag, Ga, Zn etc.) load with aromatization activity.Due to the acidity that ZSM-5 molecular sieve is stronger, excellent hydrothermal stability and most important duct shape selectivity, make ZSM-5 molecular sieve be widely used in aromatization.And Zn is as metal cheap and easy to get, and the high selectivity that shows in aromatization of the ZSM-5 molecular sieve of Zn modification and prominent.Many research reports show, Zn, in aromatization, by strengthening dehydrogenation functionality acting synergistically with the acid site of molecular sieve, thus improves the aromatization activity of ZSM-5 molecular sieve and selective.
Narrow in shaping fluid catalyst technology of preparing existing, comparatively common as binding agent using polymeric aluminum chloride, its preparation flow is simple, and processing ease, slurries manufacturing cycle is short, and solid content is high.And the stability of polymeric aluminum chloride is also fine, is convenient to slurries long storage time.But containing a large amount of chlorine elements in polymeric aluminum chloride, a large amount of hydrogen chloride gas is produced in catalyst roasting process, easily cause equipment corrosion and environmental pollution, this requires that equipment has antiseptic property, and this brings certain technical difficulty to industrial production.In addition, the research of the people such as Lin Jie [petroleum journal (PETROLEUM PROCESSING) the 16th volume the 5th phase p:36-40 in 2000] also finds, when catalyst is using Al2O3 as binding agent, in high-temperature roasting and hydrothermal treatment process, Zn constituent element can move, originally be on acidic zeolite position, synergistic Zn can be formed with molecular sieve and move on Al2O3 from molecular sieve, cause the aromatization catalyst activity containing Zn to decline.And using polymeric aluminum chloride or other aluminium base Methanol arenes catalytic agent prepared as binding agent, the inevitable problem that also there is Zn and run off.
Patent CN1240814 reports a kind of manufacture method of catalyst and cracking of hydrocarbon, contain at spray drying forming forward direction in the catalyst slurry of polymeric aluminum chloride, carclazyte and Y zeolite and add Ludox or Silica hydrogel, then spraying dry, washing is carried out, obtain finished catalyst after oven dry, decrease the discharge of hydrogen chloride gas.
Patent CN1417297 reports a kind of silica-based semi-synthetic Hydrocarban coversion catalysts containing rare earth, be characterized in the catalyst be made up of the silica sol binder containing rare earth salts, natural aluminium silicate clay and Prof. Du Yucang molecular sieve, improve heavy oil cracking activity and preventing from heavy metal pollution ability.
Patent CN 1552801 reports a kind of catalytic cracking catalyst and preparation method thereof, and it is made up of clay, Ludox, boehmite, molecular sieve and hybrid metal.The compound binding agent that it adopts Ludox and part boehmite to combine, not only enhances the macromolecular cleavage ability of catalyst, ensures that again it has good anti-wear performance simultaneously.
Patent US3957689 reports a kind of catalytic cracking catalyst.The pH value of sulfuric acid/aluminum sulfate cushioning liquid adjustment sodium metasilicate is adopted then to add clay, molecular sieve to lower scope, make catalyst by spraying dry.Gained catalyst has higher reactivity and higher anti-wear performance.
Patent US4987110 reports a kind ofly has stronger anti-wear performance and the catalytic cracking catalyst compared with high selectivity.And the binding agent that it adopts is Ludox and polymeric aluminum chloride compound binding agent.
Summary of the invention
One of technical problem to be solved by this invention is the technical problem that the Zn constituent element in the fluid catalyst of Methanol aromatic hydrocarbons easily runs off in catalyst roasting and hydrothermal treatment process, there is provided a kind of Methanol aromatic hydrocarbons fluid catalyst containing Zn, this catalyst has the advantage that Zn not easily runs off.
Two of technical problem to be solved by this invention is to provide a kind of method for preparing catalyst corresponding with one of technical solution problem.
Three of technical problem to be solved by this invention is to provide a kind of purposes of the catalyst corresponding with technical solution problem one.
In order to technical solution problem one, the technical solution used in the present invention is as follows: a kind of Methanol aromatic hydrocarbons fluid catalyst containing Zn, comprises following component by weight percentage:
1) binding agent of 10.0 ~ 40.0%;
2) aluminosilicate matrix of 20.0 ~ 55.0%;
3) the HZSM-5 molecular sieve of 20.0 ~ 70.0%;
4) ZnO of 0.1 ~ 10%;
Wherein binding agent is selected from silicon-containing material.
In technique scheme, preferred technical scheme is, binding agent is selected from least one in Ludox, waterglass or sodium metasilicate.And in use need to use the pH value of inorganic acid adjustment binding agent in 1.5 ~ 5.0 scopes.Described inorganic acid can be one or more in sulfuric acid, hydrochloric acid, nitric acid or phosphoric acid.Described alumino-silicate is selected from least one in kaolin, galapectite, diatomite, bentonite or sepiolite.Described ZSM-5 molecular sieve is the H type ZSM-5 molecular sieve that the ZSM-5 molecular sieve of Prof. Du Yucang obtains after ammonium exchange, roasting, and its sial atomic ratio Si/Al is 10 ~ 100, and Si/Al preferably is 10 ~ 50.ZnO in technique scheme is for adopting infusion process load on ZSM-5 molecular sieve, and its presoma is selected from least one in zinc chloride, zinc nitrate, zinc sulfate or zinc acetate.
For technical solution problem two, the technical solution used in the present invention is as follows: the preparation method of described Methanol aromatic hydrocarbons fluid catalyst, comprises following step:
1) take the ZSM-5 molecular sieve of a certain amount of H type, adopt infusion process a certain amount of ZnO of load over a molecular sieve, then through 80 ~ 120 DEG C of drying 8 ~ 24h, 500 ~ 650 DEG C of roasting 2 ~ 8h are for subsequent use;
2) take a certain amount of binding agent to mix with water and be made into slurries, and by between the pH value range that adds inorganic acid adjustment slurries to 1.5 ~ 5.0;
3) alumino-silicate is added 2) in the slurries prepared, and the 10 ~ 60min that pulls an oar;
4) by 1) in the ZnHZSM-5 molecular sieve of preparation join in slurries, continue making beating 10 ~ 60min;
5) adopt spray-dired method to be prepared into micro-spherical catalyst in slurries, and through super-dry, 500 ~ 650 DEG C of roasting 2 ~ 8h obtain Methanol aromatic hydrocarbons fluid catalyst.
In technique scheme, preferred technical scheme is, between the pH value range adjusting described binding agent with inorganic acid to 2.0 ~ 5.0, wherein inorganic acid is selected from least one in sulfuric acid, hydrochloric acid, nitric acid or phosphoric acid.Rate-determining steps 3) in the grain graininess of slurry be 1-20 μm.
Methanol aromatic hydrocarbons fluid catalyst provided by the invention, owing to using based binder, therefore avoids and introduce Al in forming process
2o
3, prevent Zn constituent element to move to Al from molecular sieve surface in catalyst roasting and hydrothermal treatment process
2o
3problem.Meanwhile, before using at binding agent, by adjusting the pH value of binding agent, improve the stability of binding agent, avoiding the gathering of silica self, ensure that catalyst has stronger anti-wear performance.Meanwhile, with use polymeric aluminum chloride as binding agent Kaolinite Preparation of Catalyst method compared with, the present invention avoid or reduces the discharge of hydrogen chloride gas, reduces environmental pollution and the corrosion to equipment, achieves good technique effect.
Below by specific embodiment, the present invention is further elaborated.But the present invention is not limited in these embodiments.
Detailed description of the invention
[embodiment 1]
Taking 1500g silica alumina ratio Si/Al is the ZSM-5 molecular sieve of 30, and the aqueous ammonium nitrate solution being 5% with 6000g concentration mixes.Under 90 DEG C of conditions, add thermal agitation 2h, filter, wash.After repeating said process twice, filter cake is placed in 120 DEG C of oven drying 12h, then 550 DEG C of roasting 4h obtain the ZSM-5 molecular sieve of H type.
Get the HZSM-5 molecular sieve that 800g said method is obtained, with 1200g zinc nitrate (ZnO mass concentration is 3.3%) aqueous solution, fully after mixing through super-dry, 550 DEG C of roasting 4h obtain the HZSM-5 molecular sieve containing Zn.
Get 100g Guangzhou Ludox (SiO2 mass concentration 40%, ammonium is steady), add the sulfuric acid that 11g concentration is 5%, adjusted to ph is to 2.0.Add the slurries that 500g water and 100g kaolin mix, adopt colloid mill strongly to mix 20min.Add the HZSM-5 molecular sieve containing Zn of the above-mentioned preparation of 100g again, continuation colloid mill mixes 20min strongly.Adopt spray-dired method to be prepared into micro-spherical catalyst in the slurries mixed, and at 100 DEG C of dry 16h, 600 DEG C of roasting 4h obtain Methanol aromatic hydrocarbons fluid catalyst A.
[embodiment 2]
Get 10.0g red fuming nitric acid (RFNA), mix with 200g waterglass (SiO2 concentration 20%) after adding the dilution of 40g water, obtain the mixed liquor that pH value is 2.2.Getting after 100g diatomite mixes with 200g water adds in waterglass, adopts colloid mill strongly to mix 15min.Get the HZSM-5 molecular sieve containing Zn of preparation in 100g embodiment 1, join in mixed serum, continue glue mill 30min.Spray-dired method is adopted to be prepared into micro-spherical catalyst in the slurries mixed, and at 120 DEG C of dry 12h, 580 DEG C of roasting 6h.Catalyst is washed, removes Na ion, after drying, namely obtain Methanol aromatic hydrocarbons fluid catalyst B.
[embodiment 3]
Get 80g Guangzhou Ludox (SiO2 mass concentration 40%, ammonium is steady), after adding the dilution of 320g water, be added dropwise to 15g SPA.Taking 100g bentonite subsequently adds in Ludox, adopts colloid mill strongly to mix 30min, then adds the HZSM-5 molecular sieve containing Zn of preparation in 90g embodiment 1, joins in mixed serum, continues glue mill 30min.Adopt spray-dired method to be prepared into micro-spherical catalyst in the slurries mixed, and at 110 DEG C of dry 18h, 620 DEG C of roasting 4h obtain Methanol aromatic hydrocarbons fluid catalyst C.
[embodiment 4]
Get 80g sodium metasilicate, be dissolved in 160g water, add the sulfuric acid that 280g concentration is 15% inward, after mixing, add 80g kaolin, adopt colloid mill strongly to mix 10min.Add the HZSM-5 molecular sieve containing Zn of preparation in 70g embodiment 1 again, join in mixed serum, continue glue mill 30min.Adopt spray-dired method to be prepared into micro-spherical catalyst in the slurries mixed, and at 100 DEG C of dry 18h, 650 DEG C of roasting 4h obtain Methanol aromatic hydrocarbons fluid catalyst D.
[embodiment 5 ~ 7]
Getting the HZSM-5 molecular sieve of preparation in 100g embodiment 1, take zinc nitrate solution as maceration extract loading ZnO.Make the ZSM-5 molecular sieve containing Zn that ZnO content is 1.0%, 3.0%, 8.0% respectively.
According to the method for embodiment 1, adopt ZnO content in the ZSM-5 molecular sieve alternate embodiment 1 of above-mentioned different ZnO content to be the ZSM-5 molecular sieve of 5.0% respectively, be prepared into Methanol aromatic hydrocarbons fluid catalyst E, F and G.
[embodiment 8]
Taking 600g silica alumina ratio Si/Al is the ZSM-5 molecular sieve of 60, and the aqueous ammonium chloride solution being 10 with 3000g concentration mixes.Add thermal agitation 1.5h under 90 DEG C of conditions, filter, wash.After repeating said process twice, filter cake is placed in 120 DEG C of oven drying 10h, then 540 DEG C of roasting 6h obtain the ZSM-5 molecular sieve of H type.
Get HZSM-5 molecular sieve prepared by 600g said method, mix with 360g solution of zinc sulfate (ZnO mass concentration is 5.2%), after drying, 530 DEG C of roasting 5h obtain the ZSM-5 molecular sieve containing Zn.
Get 220g Guangzhou Ludox (SiO2 mass concentration 40%, ammonium is steady), the dilute sulfuric acid being 0.1% with 700g concentration mixes, and then adds 240g kaolin and is mixed into slurries, adopts colloid mill strongly to mix 20min.Add the HZSM-5 molecular sieve containing Zn prepared by 200g said method again, continuation colloid mill mixes 50min strongly.Adopt spray-dired method to be prepared into micro-spherical catalyst in the slurries mixed, and at 120 DEG C of dry 8h, 640 DEG C of roasting 4h obtain Methanol aromatic hydrocarbons fluid catalyst H.
[embodiment 9]
Get the catalyst H of preparation in 150g embodiment 8, be placed in fixed fluidized-bed reactor.Adopt water pump with the speed of 2.5g/min toward water flowing in reactor.Before entering reactor, water need be gasified by preheating device.The temperature that catalyst contacts with water is 550 DEG C, and time of contact is 8h.Stop water flowing subsequently, catalyst is dry, obtain Methanol aromatic hydrocarbons fluid catalyst I.
[comparative example 1]
Get 420g Alumina gel (Al2O3 mass concentration is 21%), add the slurries that 480g water and 240g kaolin are mixed into, adopt colloid mill strongly to mix 20min.Add the HZSM-5 molecular sieve containing Zn of preparation in 200g embodiment 8 again, continuation colloid mill mixes 50min strongly.Adopt spray-dired method to be prepared into micro-spherical catalyst in the slurries mixed, and at 120 DEG C of dry 8h, 640 DEG C of roasting 4h obtain Methanol aromatic hydrocarbons fluid catalyst J.
[comparative example 2]
Get the catalyst J of preparation in 150g comparative example 1, be placed in fixed fluidized-bed reactor.Adopt water pump with the speed of 2.5g/min toward water flowing in reactor.Before entering reactor, water need be gasified by preheating device.The temperature that catalyst contacts with water is 550 DEG C, and time of contact is 8h.Stop water flowing subsequently, catalyst is dry, obtain Methanol aromatic hydrocarbons fluid catalyst K.
Catalyst prepared by this experiment carries out performance evaluation on fixed fluidized-bed reactor, and experiment condition is reaction temperature 430 DEG C, mass space velocity=1.0h
-1, normal pressure, the reaction time is under the reaction condition of 1h, and the Methanol aromatic hydrocarbons reaction result of each catalyst is listed in table 1, and wherein BTX representative represents benzene, toluene and dimethylbenzene respectively.
Table 1
| Embodiment | Catalyst | Aromatics quality yield/% | BTX mass yield/% |
| Embodiment 1 | A | 59.7 | 48.2 |
| Embodiment 2 | B | 58.7 | 48.0 |
| Embodiment 3 | C | 56.3 | 45.7 |
| Embodiment 4 | D | 56.7 | 46.2 |
| Embodiment 5 | E | 52.4 | 43.0 |
| Embodiment 6 | F | 55.2 | 44.9 |
| Embodiment 7 | G | 61.7 | 48.9 |
| Embodiment 8 | H | 53.6 | 40.2 |
| Embodiment 9 | I | 47.4 | 36.5 |
| Comparative example 1 | J | 50.5 | 39.1 |
| Comparative example 2 | K | 45.4 | 35.9 |
Claims (10)
1., containing a Methanol aromatic hydrocarbons fluid catalyst of Zn, comprise following component by weight percentage:
1) binding agent of 10.0 ~ 40.0%;
2) aluminosilicate matrix of 20.0 ~ 55.0%;
3) the HZSM-5 molecular sieve of 20.0 ~ 70.0%;
4) ZnO of 0.1 ~ 10%;
Wherein binding agent is selected from silicon-containing material.
2. Methanol aromatic hydrocarbons fluid catalyst according to claim 1, is characterized in that described binding agent is selected from least one in Ludox, waterglass or sodium metasilicate.
3. Methanol aromatic hydrocarbons fluid catalyst according to claim 1, is characterized in that described aluminosilicate matrix is selected from least one in kaolin, galapectite, diatomite, bentonite or sepiolite.
4. Methanol aromatic hydrocarbons fluid catalyst according to claim 1, is characterized in that described HZSM-5 molecular sieve sial atomic ratio Si/Al is 10 ~ 100.
5. Methanol aromatic hydrocarbons fluid catalyst according to claim 1, is characterized in that the presoma of described ZnO is selected from least one in zinc chloride, zinc nitrate, zinc sulfate or zinc acetate.
6. the preparation method of Methanol aromatic hydrocarbons fluid catalyst described in claim 1, comprises following step:
1) take the ZSM-5 molecular sieve of a certain amount of H type, adopt infusion process a certain amount of ZnO of load over a molecular sieve, then through 80 ~ 120 DEG C of drying 8 ~ 24h, 500 ~ 650 DEG C of roasting 2 ~ 8h are for subsequent use;
2) take a certain amount of binding agent to mix with water and be made into slurries, and by between the pH value range that adds inorganic acid adjustment slurries to 1.5 ~ 5.0;
3) aluminosilicate matrix is added 2) in the slurries prepared, and the 10 ~ 60min that pulls an oar;
4) by 1) in the HZSM-5 molecular sieve of load Zn of preparation join in slurries, continue making beating 10 ~ 60min;
5) adopt spray-dired method to be prepared into micro-spherical catalyst in slurries, and through super-dry, 500 ~ 650 DEG C of roasting 2 ~ 8h obtain Methanol aromatic hydrocarbons fluid catalyst.
7. the preparation method of Methanol aromatic hydrocarbons fluid catalyst according to claim 6, between the pH value range that it is characterized in that adjusting described binding agent with inorganic acid to 2.0 ~ 5.0, wherein inorganic acid is selected from least one in sulfuric acid, hydrochloric acid, nitric acid or phosphoric acid.
8. the preparation method of Methanol aromatic hydrocarbons fluid catalyst according to claim 7, is characterized in that rate-determining steps 3) in the grain graininess of slurry be 1-20 μm.
9. a method for Methanol aromatic hydrocarbons, taking methyl alcohol as raw material, is 300 ~ 600 DEG C in reaction temperature, reaction pressure 0.01 ~ 1MPa, and methanol weight air speed is 0.1 ~ 8h
-1, water/methanol weight ratio is under the condition of 0 ~ 5, and raw material is by any one catalyst exposure in beds and claim 1 ~ 5, and reaction generates the product based on aromatic hydrocarbons.
10. the method for Methanol aromatic hydrocarbons according to claim 9, taking methyl alcohol as raw material, is 350 ~ 550 DEG C in reaction temperature, reaction pressure 0.1 ~ 1MPa, and methanol weight air speed is 0.2 ~ 6h
-1, water/methanol weight ratio is under the condition of 0.5 ~ 4, and raw material is by beds, and reaction generates the product based on aromatic hydrocarbons.
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Cited By (9)
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| CN106607079A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Methanol-to-aromatic hydrocarbon catalyst and uses tehreof |
| CN106607076A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Catalyst for preparing arene from methyl alcohol and preparation method of catalyst |
| CN107010639A (en) * | 2017-04-11 | 2017-08-04 | 四川润和催化新材料股份有限公司 | A kind of molecular sieves of multi-stage porous ZSM 5 and preparation method thereof and the method for preparing MTA catalyst |
| CN109701598A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | Methanol arenes catalytic agent and application thereof |
| CN109701599A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | The catalyst of methanol aromatic hydrocarbons and application thereof method |
| CN109701597A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | Methanol arenes catalytic agent of high hydrothermal stability and application thereof |
| CN109701622A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | The fluid catalyst of methanol aromatic hydrocarbons |
| CN109071377B (en) * | 2016-04-28 | 2021-07-13 | 旭化成株式会社 | Method for producing aromatic hydrocarbon-containing compound |
| CN116328752A (en) * | 2022-12-13 | 2023-06-27 | 中国科学院大连化学物理研究所 | Catalyst, preparation method and application of catalyst in preparation of propylene carbonate |
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| CN106607079A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Methanol-to-aromatic hydrocarbon catalyst and uses tehreof |
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| CN109071377B (en) * | 2016-04-28 | 2021-07-13 | 旭化成株式会社 | Method for producing aromatic hydrocarbon-containing compound |
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| CN109701622A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | The fluid catalyst of methanol aromatic hydrocarbons |
| CN109701597A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | Methanol arenes catalytic agent of high hydrothermal stability and application thereof |
| CN109701599A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | The catalyst of methanol aromatic hydrocarbons and application thereof method |
| CN109701598B (en) * | 2017-10-26 | 2022-04-05 | 中国石油化工股份有限公司 | Catalyst for preparing aromatic hydrocarbon from methanol and application thereof |
| CN109701599B (en) * | 2017-10-26 | 2022-07-08 | 中国石油化工股份有限公司 | Catalyst for preparing aromatic hydrocarbon from methanol and application method thereof |
| CN109701597B (en) * | 2017-10-26 | 2022-07-12 | 中国石油化工股份有限公司 | Methanol-to-aromatic hydrocarbon catalyst with high hydrothermal stability and application thereof |
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