CN102744066A - Nitrobenzene hydrogenation aniline preparation catalyst for fluidized bed - Google Patents
Nitrobenzene hydrogenation aniline preparation catalyst for fluidized bed Download PDFInfo
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- CN102744066A CN102744066A CN2012101397476A CN201210139747A CN102744066A CN 102744066 A CN102744066 A CN 102744066A CN 2012101397476 A CN2012101397476 A CN 2012101397476A CN 201210139747 A CN201210139747 A CN 201210139747A CN 102744066 A CN102744066 A CN 102744066A
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Abstract
The present invention belongs to the technical field of catalyst preparation, and provides a nitrobenzene hydrogenation aniline preparation catalyst for a fluidized bed. The catalyst provided by the present invention has the following characteristics that: composition is single, the catalyst only contains an active ingredient copper, introduction of a multi-element component to the catalyst is not required, and physicochemical properties of the catalyst are: an average specific surface area of 350-500 m<2>/g, an average pore size of 2.5-4.0 nm, and an average pore volume of 0.55-0.85 ml/g. In addition, a mass content of the active ingredient copper in the catalyst is 10-25%; a mass percentage of the catalyst with particle size distribution of 125-600 mum is 80-98%, and a mass percentage of the catalyst with particle size distribution less than 125 mum is less than 2%; and the catalyst has characteristics of high activity, uneasy pore clogging, long service life, high selectivity, and the like.
Description
Technical field
The invention belongs to catalyst technical field, be specifically related to a kind of fluid bed and use the manufacturing process of aniline through nitrobenzene hydrogenation catalyst.
Background technology
As everyone knows, the catalyst system that is used for the nitrobenzene gas phase hydrogenation has copper system, nickel system and noble metal system etc.Catalyst carrier has silica gel, zeolite, activated alumina and diatom scholar etc.Copper catalyst has higher activity and selectivity; Raney nickel is often processed the multielement composite catalyst, to keep the high selectivity and the activity of reaction, avoids benzene ring hydrogenation.In concrete the production, adopt fixed bed or fluidized-bed reactor usually.
For fluid bed with the manufacturing process of aniline through nitrobenzene hydrogenation catalyst; Normally will contain the method that the salt of active constituent impregnated on the carrier makes; Wherein active constituent adopts copper usually or on the basis of copper, adds some other auxiliary agent, and carrier adopts silochrom usually.
US5,304,525, US6,818,720 provide a kind of noble metal catalyst that is used for the nitrobenzene gas phase hydrogenation respectively, and active constituent is mainly Pt, Ru etc.
US3,504,035 provide a kind of Cu-Si or Cu-Al catalyst, and Cr, Ba, Zn etc. carry out modification, catalyst particle size 200 μ m ~ 400 μ m.Adopt fluid bed gas phase hydrogenation method, 250 ℃ ~ 300 ℃ of reaction temperatures, reaction pressure 0.4MPa ~ 1.0MPa, the mol ratio of nitrobenzene and hydrogen is 1: 3, the initial yield of aniline is greater than 99%.
CN1657162A is a carrier through adopting with silica, is Cu with the chemical formula
aCr
bMo
cA
dO
x, wherein A is selected from least a technical scheme among Ni, Zn, Ba, V, Bi, Pb or the Pd, can be used in the commercial production of manufacturing process of aniline through nitrobenzene hydrogenation.
CN 1301154C provide a kind of reproducible hydrogenation catalyst and preparation method thereof, and it is at SiO
2One or more active components on the carrier among loaded Cu, Fe, CO, Ni, Cr, Mn, the Mo are formed; Catalyst is by any the making in the precipitation method, coprecipitation and the infusion process; Catalyst is effective especially to the hydrogenation of aromatic hydrocarbon nitro compound; Catalyst life is to have catalyst now more than one times, and catalyst can carry out hydrogenation reaction under normal pressure (or pressurization), though method for preparing catalyst is fairly simple.But because component is many, various component adsorption properties are different, and the catalyst of therefore preparing is formed not temperature, are unfavorable for producing in batches.
For the catalyst of the manufacturing process of aniline through nitrobenzene hydrogenation of copper silicon system; Its active component Cu its nitrobenzene conversion ratio under lower content just can reach more than 99.99%; Key is how to control reaction speed, prevents the duct obstruction, prolongs catalyst life; Increase the wear-resisting performance of catalyst simultaneously, can reduce the unit consumption of catalyst in the Aniline Production process.These all need catalyst that proper pore structure and size distribution ratio are arranged.
Summary of the invention
The object of the present invention is to provide a kind of fluid bed to use the manufacturing process of aniline through nitrobenzene hydrogenation catalyst; Proper pore structure and size distribution ratio have been characterized in; Make catalyst have high activity and selectivity; Simultaneously the catalyst one way life-span long, greatly reduce in the Aniline Production process consumption to catalyst.
The mass content of catalyst activity component copper according to the invention is 10% ~ 25%, and moisture mass ratio is 0.5% ~ 5%, and all the other are silica gel.Catalyst is formed simple, and preparation stability is stronger, and catalyst has long service life, characteristics such as active height, selectivity height.
Usually, silica gel is stated and is the gross porosity microsphere silica gel.Typical gross porosity microsphere silica gel physical and chemical performance: specific surface is 363.6m
2/ g, pore volume are 0.87ml/g, and average pore size is 4.8nm.
The average BET 350m of said catalyst characteristics
2/ g ~ 500 m
2/ g, average pore size 2.5nm ~ 4.0nm, average pore volume 0.55ml/g ~ 0.85ml/g.
The mass particle ratio of the size distribution of said catalyst between 125 μ m ~ 600 μ m is 80% ~ 98%; Wherein the mass particle ratio less than 125 μ m is lower than 0 ~ 2%; Particle between 125 μ m ~ 250 μ m is than 9% ~ 20%; Particle between 250 μ m ~ 600 μ m is than 70% ~ 85%, greater than the particle of 600 μ m than 0.5% ~ 20%.
The average BET:380m of said catalyst
2/ g ~ 460 m
2/ g, average pore size 2.5nm ~ 3.8nm, average pore volume 0.60ml/g ~ 0.82ml/g, wherein pore-size distribution is that 0 ~ 2nm ratio is 10% ~ 22%, and 2nm ~ 5nm ratio is 50% ~ 80%, and 5nm ~ 10nm ratio is 8% ~ 35%, is 0.5% ~ 2% greater than the 10nm ratio.
It is that mass ratio is 80% ~ 98% between 125 μ m ~ 600 μ m that the present invention provides the size distribution of catalyst, is lower than 2% less than the mass particle ratio of 125 μ m.Greatly reduce the catalyst loss that catalyst in use causes owing to wearing and tearing, therefore also reduced the catalyst consumption in the Aniline Production process.
Catalyst preparation process of the present invention is: the cupric ammine complex solution that adding ammoniacal liquor is made into clarification in the copper nitrate solution that contains the catalyst activity component is as maceration extract; Silica-gel carrier joins in the reactor of cupric ammine complex solution and floods then; Ground stirred 2 ~ 5 hours under 70 ℃ ~ 90 ℃ temperature; Dipping after accomplishing separates solid-liquid, and solid particle is through washing, be drying to obtain the catalyst finished product.
Catalyst of the present invention also has the selectivity height having under the active high prerequisite, has lowered generation, the especially low-boiling-point substance of side reaction in the Aniline Production process.This catalyst has the duct and is difficult for characteristics such as obstruction, long service life, anti-wear performance height.
Catalyst ratio of components provided by the invention is more single, only contains active ingredient copper, need not in catalyst, to introduce multicomponent mixture, makes Preparation of Catalyst be more prone to, and the production control of catalyst is also more stable.
The specific embodiment
Be elaborated through embodiment below.The purpose of enumerating these instances is just in order to explain the present invention, rather than limitation of the present invention.
Carrier of the present invention and Preparation of Catalyst are implemented according to following steps.The physical and chemical performance of used gross porosity microsphere silica gel is: specific surface is 363.6m
2/ g, pore volume are 0.87ml/g, and average pore size is 4.8nm.
Embodiment 1
Preparation of Catalyst is in closed reactor, to carry out, and several steps below pressing implement.1. prepare cuprammonia: the ammoniacal liquor of getting 100ml10M joins in the copper nitrate solution of 500ml 0.5M, is mixed with the cupric ammine complex solution of clarification, adds 600 ml ionized waters again and stirs.2. flood: get 200g silica gel and join in the cupric ammine complex solution 1., under stirring, vacuumize maintenance 3 hours at 70 ℃, dipping is accomplished.3. separate, washing, drying: will flood material and carry out Separation of Solid and Liquid, solid material to neutral, carries out drying through washing again, the catalyst finished product.This catalyst copper content is 15.5%, specific surface 380.5m
2/ g, pore volume 0.72ml/g, average pore size 3.5nm.
Embodiment 2
Preparation of Catalyst is in closed reactor, to carry out, and several steps below pressing implement.1. prepare cuprammonia: the ammoniacal liquor of getting 200ml10M joins in the copper nitrate solution of 500ml 0.5M, is mixed with the cupric ammine complex solution of clarification.2. flood: get 200g silica gel and join in the cupric ammine complex solution 1., stir down at 90 ℃ and vacuumize maintenance 4 hours, the dipping completion.3. separate, washing, drying: will flood material and carry out Separation of Solid and Liquid, solid material to neutral, carries out drying through washing again, the catalyst finished product.This catalyst copper content is 19.5%, specific surface 445.4m
2/ g, pore volume 0.82ml/g, average pore size 3.8nm.
Embodiment 3
Preparation of Catalyst is in closed reactor, to carry out, and several steps below pressing implement.1. prepare cuprammonia: the ammoniacal liquor of getting 100ml10M joins in the copper nitrate solution of 500ml 0.5M, is mixed with the cupric ammine complex solution of clarification.2. flood: get 200g silica gel and join in the cupric ammine complex solution 1., under 80 ℃ of stirrings, vacuumize maintenance 4 hours, dipping is accomplished.3. separate, washing, drying: will flood material and carry out Separation of Solid and Liquid, solid material to neutral, carries out drying through washing again, the catalyst finished product.This catalyst copper content is 20.6%, specific surface 463.5m
2/ g, pore volume 0.63ml/g, average pore size 3.1nm.
Embodiment 4
Preparation of Catalyst is in closed reactor, to carry out, and several steps below pressing implement.1. prepare cuprammonia: the ammoniacal liquor of getting 100ml10M joins in the copper nitrate solution of 500ml 0.5M, is mixed with the cupric ammine complex solution of clarification, adds 400 ml ionized waters again and stirs.2. flood: get 200g silica gel and join in the cupric ammine complex solution 1., under 80 ℃ of stirrings, vacuumize maintenance 5 hours, dipping is accomplished.3. separate, washing, drying: will flood material and carry out Separation of Solid and Liquid, solid material to neutral, carries out drying through washing again, the catalyst finished product.This catalyst copper content is 18.3%, specific surface 498.5m
2/ g, pore volume 0.56ml/g, average pore size 2.6nm.
Embodiment 5
Preparation of Catalyst is in closed reactor, to carry out, and several steps below pressing implement.1. prepare cuprammonia: the ammoniacal liquor of getting 100ml10M joins in the copper nitrate solution of 500ml 0.5M, is mixed with the cupric ammine complex solution of clarification, adds 200 ml ionized waters again and stirs.2. flood: get 200g silica gel and join in the cupric ammine complex solution 1., under 75 ℃ of stirrings, vacuumize maintenance 4 hours,, dipping is accomplished.3. separate, washing, drying: will flood material and carry out Separation of Solid and Liquid, solid material to neutral, carries out drying through washing again, the catalyst finished product.This catalyst copper content is 19.6%, specific surface 412.7m
2/ g, pore volume 0.71ml/g, average pore size 3.4nm.
Catalyst sample with embodiment 1～5 preparation carries out activity rating in fluidized-bed reactor, be 3.0h in raw material nitrobenzene liquid air speed
-1, control 200 ℃ of reaction temperatures, hot(test)-spot temperature be to carry out activity rating under 280 ℃ the condition, when the nitrobenzene residual volume is higher than 100ppm, as the single test terminal point, investigates the catalyst continuous operating time, the result sees the following form.
Table 1 catalyst activity and pore-size distribution
Table 2 catalyst grain size distributes
| Sample | ＜125μm/% | ?125～250μm/% | ?250～600μm/% | ＞600μm/% |
| Embodiment 1 | 0 | 17.49 | 80.11 | 2.40 |
| Embodiment 2 | 0.85 | 14.41 | 70.58 | 14.16 |
| Embodiment 3 | 1.47 | 9.16 | 70.85 | 18.51 |
| Embodiment 4 | 2.21 | 16.83 | 82.50 | 8.46 |
| Embodiment 5 | 2.98 | 19.55 | 76.88 | 0.59 |
Claims (7)
1. a fluid bed is used the manufacturing process of aniline through nitrobenzene hydrogenation catalyst, and the mass content that it is characterized in that activity of such catalysts component copper is 10% ~ 25%, and moisture mass ratio is 0.5% ~ 5%, and all the other are silica gel.
2. catalyst as claimed in claim 1 is characterized in that the said silica gel of catalyst is the gross porosity microsphere silica gel.
3. catalyst as claimed in claim 2, the specific surface that it is characterized in that the gross porosity microsphere silica gel is 363.6m
2/ g, pore volume are 0.87ml/g, and average pore size is 4.8nm.
4. catalyst as claimed in claim 1 is characterized in that the average BET 350m of catalyst
2/ g ~ 500 m
2/ g, average pore size 2.5nm ~ 4.0nm, average pore volume 0.55ml/g ~ 0.85ml/g.
5. catalyst as claimed in claim 1; The mass particle ratio of size distribution between 125 μ m ~ 600 μ m that it is characterized in that catalyst is 80% ~ 98%; Wherein the mass particle ratio less than 125 μ m is lower than 0 ~ 2%; Particle between 125 μ m ~ 250 μ m is than 9% ~ 20%, and the particle between 250 μ m ~ 600 μ m is than 70% ~ 85%, greater than the particle of 600 μ m than 0.5% ~ 20%.
6. catalyst as claimed in claim 1 is characterized by average BET:380m
2/ g ~ 460 m
2/ g, average pore size 2.5nm ~ 3.8nm, average pore volume 0.60ml/g ~ 0.82ml/g, wherein pore-size distribution is that 0 ~ 2nm ratio is 10% ~ 22%, and 2nm ~ 5nm ratio is 50% ~ 80%, and 5nm ~ 10nm ratio is 8% ~ 35%, is 0.5% ~ 2% greater than the 10nm ratio.
7. Preparation of catalysts method according to claim 1; It is characterized in that the preparation process is following: the cupric ammine complex solution that adding ammoniacal liquor is made into clarification in the copper nitrate solution that contains the catalyst activity component is as maceration extract; Then silica-gel carrier is joined in the reactor of cupric ammine complex solution and flood; Under 70 ℃ ~ 90 ℃ temperature, stirred 2 ~ 5 hours, dipping after accomplishing separates solid-liquid, and solid particle is through washing, be drying to obtain the catalyst finished product.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104098473A (en) * | 2013-04-08 | 2014-10-15 | 中国石油化工股份有限公司 | Post-treatment method of aniline |
| CN106914255A (en) * | 2017-03-29 | 2017-07-04 | 国家纳米科学中心 | A kind of non-alloyed metal composite and its preparation method and application |
| CN112536033A (en) * | 2019-09-20 | 2021-03-23 | 中石化南京化工研究院有限公司 | Catalyst for preparing o-toluidine by hydrogenation of o-nitrobenzene and preparation method thereof |
| CN112958097A (en) * | 2021-02-08 | 2021-06-15 | 清华大学 | Copper-based supported catalyst for synthesizing aniline by nitrobenzene hydrogenation and preparation method thereof |
| CN115532300A (en) * | 2021-06-29 | 2022-12-30 | 中石化南京化工研究院有限公司 | Catalyst for preparing aniline by nitrobenzene hydrogenation, preparation method and application |
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| CN1266085A (en) * | 2000-02-03 | 2000-09-13 | 中国石油天然气股份有限公司兰州石化分公司 | Selective hydrogenation catalyst for pyrolysis gasoline |
| CN101049562A (en) * | 2007-05-11 | 2007-10-10 | 清华大学 | Catalyst for preparing halogeno anilin through catalytic hydrogenation of halogeno nitrobenzene and preparation method |
| CN102000612A (en) * | 2009-09-02 | 2011-04-06 | 南化集团研究院 | Carrier of nitrobenzene hydrogenation catalyst for making aniline for fluidized bed and preparation method of catalyst |
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2012
- 2012-05-08 CN CN2012101397476A patent/CN102744066A/en active Pending
Patent Citations (3)
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| CN1266085A (en) * | 2000-02-03 | 2000-09-13 | 中国石油天然气股份有限公司兰州石化分公司 | Selective hydrogenation catalyst for pyrolysis gasoline |
| CN101049562A (en) * | 2007-05-11 | 2007-10-10 | 清华大学 | Catalyst for preparing halogeno anilin through catalytic hydrogenation of halogeno nitrobenzene and preparation method |
| CN102000612A (en) * | 2009-09-02 | 2011-04-06 | 南化集团研究院 | Carrier of nitrobenzene hydrogenation catalyst for making aniline for fluidized bed and preparation method of catalyst |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104098473A (en) * | 2013-04-08 | 2014-10-15 | 中国石油化工股份有限公司 | Post-treatment method of aniline |
| CN106914255A (en) * | 2017-03-29 | 2017-07-04 | 国家纳米科学中心 | A kind of non-alloyed metal composite and its preparation method and application |
| CN112536033A (en) * | 2019-09-20 | 2021-03-23 | 中石化南京化工研究院有限公司 | Catalyst for preparing o-toluidine by hydrogenation of o-nitrobenzene and preparation method thereof |
| CN112958097A (en) * | 2021-02-08 | 2021-06-15 | 清华大学 | Copper-based supported catalyst for synthesizing aniline by nitrobenzene hydrogenation and preparation method thereof |
| CN115532300A (en) * | 2021-06-29 | 2022-12-30 | 中石化南京化工研究院有限公司 | Catalyst for preparing aniline by nitrobenzene hydrogenation, preparation method and application |
| CN115532300B (en) * | 2021-06-29 | 2023-11-28 | 中石化南京化工研究院有限公司 | Catalyst for preparing aniline by nitrobenzene hydrogenation, preparation method and application |
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Application publication date: 20121024 |