CN1327945C - Method for conducting catalytic reaction in ultragravity field - Google Patents
Method for conducting catalytic reaction in ultragravity field Download PDFInfo
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- CN1327945C CN1327945C CNB2004100736242A CN200410073624A CN1327945C CN 1327945 C CN1327945 C CN 1327945C CN B2004100736242 A CNB2004100736242 A CN B2004100736242A CN 200410073624 A CN200410073624 A CN 200410073624A CN 1327945 C CN1327945 C CN 1327945C
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Abstract
The present invention discloses a method for making a catalytic reaction in a super gravitational field, the method comprises the following steps: heterogeneous catalysts are treated to a liquid phase and then are used for the catalytic reaction which is made in a super gravitational rotary bed reactor, wherein the liquid phase treatment is that active components of catalysts are dissolved in liquid phase reaction materials or solvents to form homogeneous mixture or dispersed in the liquid phase reaction materials or solvents to form emulsion. The method of the present invention extends the period of catalyst regeneration greatly, and enhances production efficiency.
Description
Technical field
The present invention relates to a kind of method of catalytic reaction, specifically, the present invention relates to a kind of method of in super gravity field, carrying out catalytic reaction.
Background technology
The super gravity field technology is an emerging engineering, is characterized in that volume is little, mass transfer intensity height, easily operation, in recent years the super gravity field technology solved many under normal gravitational field insoluble problem.CN1064338A discloses the method for utilizing revolving bed to carry out the oil-field flooding deoxidation, successfully is applied to plant-scale separation process with high-gravity rotating bed.CN1116146A discloses a kind of method for preparing ultramicro powder under super gravity field; CN1116185A discloses and has utilized the rotating bed super gravity field device as reactor, prepares the method for calcium carbonate superfine powder; These technology successfully are applied to plant-scale preparation process with high-gravity rotating bed.
Industrial heterogeneous catalytic reaction and homogeneous catalytic reaction are used very extensive, heterogeneous catalytic reaction and homogeneous catalytic reaction exist many problems in commercial Application, main performance has: contact weak effect between catalyst and the reactant, mass transfer intensity is low, it is slow that product leaves the speed of catalyst surface, catalyst amount is big, and utilization rate is low, and life cycle is short; Easily the knot charcoal needs frequent regeneration, even also there are a lot of active components not play a role in the catalyst of inactivation.Homogeneous catalyst is owing to be difficult to separate with product, and people explored homogeneous catalyst is loaded on the carrier is the method for heterogeneousization of homogeneous catalysis, explores through research for many years, and the industrialization of being unrealized so far mainly is that the problem of loss of active component is difficult to solve.
In order to reduce the cost of heterogeneous catalyst, give full play to the effect of active component, need a kind of new catalytic reaction method of exploitation, solve above-mentioned problem.CN1507940A discloses a kind of method of catalytic reaction, first high-gravity technology is applied in the catalytic reaction, but this method is that solid catalyst is fixed on the rotor of rotating packed bed reactor, cause this method to have following shortcoming: under action of centrifugal force, liquid phase is washed away the active constituent that causes easily on the catalyst granules to catalyst and is run off; Higher to the requirement of strength of catalyst granules in addition, otherwise, the catalyst granules fragmentation under action of centrifugal force, caused easily.
Summary of the invention
The purpose of this invention is to provide a kind of new catalytic reaction method, solve and in super gravity field, carry out the problem that catalytic reaction exists.
The inventor if there are not separation problem in heterogeneous catalyst liquid phaseization or heterogeneous catalyst homogeneous phaseization, can solve problems of the prior art through discovering.And catalyst in liquid phase through after repeatedly recycling, catalyst reclaims from liquid phase or filtered method is separated from liquid phase through distillation, so not only can reduce the Preparation of catalysts cost, active component is played one's part to the full, and can reclaim noble metal, minimizing environmental pollution.
Method of the present invention is with after the heterogeneous catalyst liquid phaseization, carries out catalytic reaction in rotating packed bed reactor.
Concrete, liquid phaseization of the present invention can realize by two kinds of approach, the one, and the activity of such catalysts components dissolved is formed homogeneous mixture in liquid phase reacting material or solvent, or be dispersed in liquid phase reacting material or the solvent and form emulsion; Wherein said solvent can be at least a in water, aliphatic hydrocarbon, aromatic hydrocarbons, organic acid, alcohol, aldehyde and the ester, for example benzene or toluene.The 2nd, with heterogeneous catalyst miniaturization or ultra-fineization,, be suspended in catalyst granules in the liquid phase reacting material equably then as catalyst being made the particle of particle diameter 0.005-100 μ m; Coating of particles can be an arbitrary shape, is preferably sphere, polyhedron shape, cylindrical, truncated cone-shaped and sheet.
Method of the present invention is applicable to heterogeneous catalytic reaction and homogeneous catalytic reaction in petrochemical industry and the fine chemistry industry production; react as unsaturated hydrocarbon selective hydrogenation; the full hydrogenation reaction of unsaturated hydrocarbons; hydroformylation reaction; ammoxidation reaction; oxi-chlorination, olefinic polyreaction or hydrocarbon catalytic cracking reaction etc.Wherein said hydrogenation reaction of unsaturated hydrocarbon can be C
2-C
5Alkene or alkadienes or selective acetylene hydrocarbon hydrogenation or full hydrogenation, gasoline, diesel oil hydrogenation remove reactions such as unsaturated bond; Described olefinic polyreaction can be that part has catalyst/or initator polymerisation in solution, bulk polymerization of participating in; Described hydrocarbon catalytic cracking reaction can be the reaction or the C of naphtha, light diesel fuel or mink cell focus catalytic pyrolysis preparing ethylene, propylene
4-C
8Catalytic reactions such as olefin catalytic is preparing propylene transformed, ethene.
Heterogeneous and the homogeneous catalytic reaction that the present invention relates to, the phase of system are any combination of gas, liquid, solid three-phase, i.e. solution-air, liquid-liquid, the reaction of liquid-solid biphasic catalysis, gas-liquid-solid, liquid-liquid-solid three phase catalytic reaction, solution-air-liquid-solid heterogeneous catalytic reaction.Gas phase can be single component, also can be to contain the above mist of two components, wherein contains a certain proportion of reaction component.Liquid phase can be one-component liquid or solution, also can be mixing material or solution.Solid phase is one-component or many mixture.
Application for a patent for invention 01143459.7 discloses a kind of high-gravity rotating bed, and its structure as shown in Figure 1.The content of this patent all is incorporated herein by reference.The structure of the described rotating packed bed reactor of method of the present invention is similar to it, all is made up of housing, rotor, transmission system, sealing system and filler.But for different catalytic reactions, rotating packed bed reactor of the present invention is different.To catalytic hydrogenation reaction, the pendular ring sealing is adopted in sealing in the gas phase of reactor, and sealing fluid is from the catalytic hydrogenation product, and the position of pendular ring sealing is at outer ring such as Fig. 2 of rotor.For catalytic cracking reaction, the pendular ring sealing is adopted in sealing in the gas phase of reactor, and sealing fluid is from material liquid, and the position of pendular ring sealing is near inner ring such as Fig. 3 of rotor.Sealing to the running part of equipment can be adopted mechanical seal and magnetic drives, has eliminated dynamic sealing point.When the temperature of catalytic reaction during greater than 150 ℃, the running part of rotary drill reactor need separate and increase cooling system with reaction system, with protection bearing, magnet steel or mechanical seal, shown in the thermal insulation layer among Fig. 3 23.
Filler in the preferred described rotating packed bed reactor is selected from a kind of in wire packing, mellapak packing or the corrugated sheet-net packing.Preferred described mellapak packing or corrugated sheet-net packing be shaped as the diameter annulus identical, its pitch of waves 2-25mm, crest 1-13mm with high-gravity rotating bed rotor.To mellapak packing, be equipped with the gas balance hole of 5-20mm on the plate, percent opening is 5%-55%.
Filler in the preferred described rotating packed bed reactor is made up of the rotating compact disc of the ripply multilayer of compacting, and the thickness of wherein said video disc is 0.15-0.5mm, and the video disc interlamellar spacing is 1-20mm.
Method of the present invention has different flow processs according to different catalytic reactions, and the structure of supergravity reactor is also different.
For catalytic hydrogenation reaction, typically reaction process as shown in Figure 4: recycling catalyst enters liquid distribution trough by the liquid phase import of hypergravity field swinging bed reactor with fresh hydrogenating materials after blending tank mixes, be sprayed at then on the inner edge of rotor packing layer, under powerful action of centrifugal force, outwards move by the rotor inner edge, hydrogen after metering, gas phase import by hypergravity field swinging bed reactor enters in the reactor, enter the rotor packing layer by the rotor outer rim under pressure, after in packing layer, carrying out hydrogenation reaction with the liquid phase that contains catalyst, remaining hydrogen is discharged by the gaseous phase outlet of hypergravity swinging bed device after the mist eliminator foam removal, liquid-phase product behind the hydrogenation and catalyst enter liquid level control jar by the liquid phase outlet of hypergravity field swinging bed reactor, enter catalyst separation/or enrichment process then, separate/or concentrate after catalyst circulation use, hydrogenated products are to subsequent processing.
React for hydrocarbon catalytic cracking, its typical reaction process is as follows: recycling catalyst and fresh lysate raw material mix the back at blending tank and are entered by the liquid phase import of hypergravity field swinging bed reactor on the inner edge that liquid distribution trough is sprayed at the rotor packing layer then, under powerful action of centrifugal force, outwards move by the rotor inner edge, the dilution/or heating steam enter by centre of rotor through steam inlet, enter rotary filler layer 6 with liquid phase, gaseous products after the cracking is discharged by the gaseous phase outlet of hypergravity swinging bed device after the mist eliminator foam removal, and remaining liquid phase and catalyst are flowed out by the liquid phase outlet of hypergravity field swinging bed reactor and recycle.
The beneficial effect that method of the present invention is brought is as follows:
1, heterogeneous catalyst liquid phaseization, method for preparing catalyst is easy.
2, because the liquid phaseization of catalyst makes the oligomer and the coking of course of reaction generation be dissolved in the liquid phase, thereby prolong the regeneration period of catalyst widely, improved productivity effect.
3, owing to the powerful action of centrifugal force of super gravity field, reaction heat can promptly shift out with liquid phase, thereby makes temperature of reaction system change steadily, and the crystal grain of catalyst changes little, has prolonged life of catalyst.
4, concerning solid catalyst, because catalyst particle size is little, specific surface is big, so the catalyst activity height, and consumption can further reduce.
5, owing in hypergravity field swinging bed reactor, carry out catalytic reaction, greatly strengthened mass transport process, thereby make the disposal ability of unit interval per volume of catalyst improve tens times and even hundreds of times, catalyst consumption is reduced widely, the utilization rate of catalyst improves widely, the size of equipment reduces widely, has reduced energy consumption, has reduced the investment of equipment.
6, because the time of staying of reaction mass in hypergravity field swinging bed reactor shortens (less than 1 second), so accessory substance obviously reduces, selection of catalysts obviously improves, the quality of product obviously improves.
Description of drawings
Fig. 1 is the structural representation of common rotating packed bed reactor in the prior art.
Fig. 2 is the structural representation that the present invention is used for the rotating packed bed reactor of catalytic hydrogenation reaction.
Fig. 3 is the structural representation that the present invention is used for the rotating packed bed reactor of catalytic cracking reaction.
Fig. 4 is the schematic flow sheet that method of the present invention is used for catalytic hydrogenation reaction.
1 housing, 2 gas feeds, 3 liquid-inlets, 4 gas vents, 5 rotors, 6 packing layers, 7 gas barriers, 8 liquid distribution troughs, 9 mist eliminators, 10 pendular ring air seal sets, 11 liquid outlets, 12 bearings/or the axle sleeve bearing, 13 bearings/or axle sleeve, 14 lubricated/and cooling fluid inlet, 15 lubricated/and cooling liquid outlet, 16 driven axles, 17 driving shafts, 18 magnetic separation sleeves, 19 interior magnet steel assemblies, 20 outer steel assemblies, 21 vapor chamber, 22 fluid chamber, 23 thermal insulation layers, 24 steam inlets, 25 steam distributors.
The specific embodiment
The flow process of catalytic hydrogenation reaction is described below in conjunction with accompanying drawing 2 and accompanying drawing 4: recycling catalyst and fresh hydrogenating materials are mixed the back at blending tank and are entered liquid distribution trough 8 by the liquid phase import 3 of hypergravity field swinging bed reactor, be sprayed at then on the inner edge of rotor packing layer 6, under powerful action of centrifugal force, outwards move by the rotor inner edge, hydrogen after metering, gas phase import by hypergravity field swinging bed reactor enters in the reactor, enter rotor packing layer 6 by the rotor outer rim under pressure, after in packing layer 6, carrying out hydrogenation reaction with the liquid phase that contains catalyst, remaining hydrogen is discharged by the gaseous phase outlet of overweight machine after mist eliminator 9 foam removals, liquid-phase product behind the hydrogenation and catalyst enter liquid level control jar by the liquid phase outlet 11 of hypergravity field swinging bed reactor, enter catalyst separation/or enrichment process then, separate/or concentrate after catalyst circulation use, hydrogenated products are to subsequent processing.
Below example will illustrate further the present invention, but not thereby limiting the invention.
Embodiment 1
In hypergravity field swinging bed reactor, carry out the full hydrogenation of C4 fraction.The full hydrogenation of C4 fraction is gas-liquid-solid phase reaction, and used material is H
2, C4 fraction (component is: butane, butylene, butadiene and butine), catalyst is Pd/Al
2O
3, temperature: 10～180 ℃, pressure: 2～40atm, rotating speed 800～2100rpm.C4 air speed 10～500hr-1, hydrogen/Bu Bao is with Key (butylene+2 * butadiene+2 * butine+3 * ethylene vinyl): 1.0～1.2mol/mol, recycle ratio: 5～9: 1.
Rotating packed bed reactor adopts structure as shown in Figure 2, flow process as shown in Figure 4, the catalyst that average grain diameter 40 μ m is contained 0.4% (wt) Pd (makes Al by sol-gal process
2O
3, spray-drying obtains Al
2O
3Powder, screening obtains the carrier of average grain diameter 40 μ m, making catalyst with this carrier) 15ml is suspended in the C4 material liquid, hydrogen is tangentially introduced in the reactor by gas phase import 2, the liquid phase C4 fraction that contains catalyst sprays to the inner edge of the packing layer of rotation at a high speed by liquid distribution trough 8, inlet temperature: 35 ℃, pressure: 25atm, air speed: 60hr
-1Hydrogen/Bu Bao is with Key: 1.0mol/mol, filler adopts the woven wire of porosity 98.5%, and rotating speed 1800rpb is after the reaction, excessive hydrogen is discharged by gaseous phase outlet 4, the C4 liquid phase fraction that contains catalyst enters liquid level control jar by liquid phase outlet 11 discharges, and the C4 liquid phase fraction that contains catalyst that is come out by liquid level control jar carries out the centrifugal sedimentation separation, clear liquid after separating, be hydrogenated products to storage tank, the C4 liquid phase fraction that another part contains catalyst recycles.
Comparative Examples 1
In fixed bed reactors, carry out the full hydrogenation of C4 fraction.The full hydrogenation of C4 fraction is gas-liquid-solid phase reaction, and used material is H
2, C4 fraction (component is: butane, butylene, butadiene and butine), catalyst is 0.4% (wt) Pd/Al
2O
3, adopt two sections bed hydroprocessings, inlet temperature: 35 ℃, pressure: 30atm.C4 air speed 20hr
-1, hydrogen/Bu Bao is with Key: 1.0mol/mol, recycle ratio: 5～9: 1.
Further specify effect of the present invention below by table 1.
Reaction result behind table 1 embodiment 1 and the Comparative Examples 1 full hydrogenation
| Embodiment 1 | Comparative Examples 1 | ||||||||
| Hydrogen/Bu Bao is with Key mol/mol | Recycle ratio | Air speed 1/h | Alkane amount % (reaction back) | Residual olefin % (reaction back) | Olefin conversion % | Air speed 1/h | Alkane amount % (after the II section) | Residual olefin % (after the II section) | Olefin conversion % |
| 1.0 | 9 | 60 | 98.99 | 0.05 | 99.81 | 20 | 98.90 | 0.08 | 99.8 |
| 1.0 | 7 | 60 | 98.96 | 0.03 | 99.56 | 20 | 98.86 | 0.04 | 99.7 |
| 1.0 | 5 | 60 | 98.90 | 0.09 | 99 | 20 | 98.7 | 0.10 | 98.56 |
| 1.0 | 9 | 60 | 98.99 | 0.05 | 99.81 | 60 | 80 | 20 | 80 |
| 1.0 | 7 | 60 | 98.96 | 0.03 | 99.56 | 60 | 70 | 30 | 70 |
| 1.0 | 5 | 60 | 98.90 | 0.09 | 99 | 60 | 60 | 40 | 60 |
Claims (5)
1, a kind of method of catalytic reaction comprises after the heterogeneous catalyst liquid phaseization, is used for catalytic reaction, and this is reflected in the rotating packed bed reactor and carries out; Wherein said heterogeneous catalyst liquid phaseization be meant the activity of such catalysts components dissolved formed homogeneous mixture in liquid phase reacting material or solvent be dispersed in liquid phase reacting material or solution in form emulsion, or after heterogeneous catalyst being made the particle of particle diameter 0.005-100 μ m, be suspended in the liquid phase reacting material.
2, method according to claim 1 is characterized in that described solvent is selected from least a in water, aliphatic hydrocarbon, aromatic hydrocarbons, organic acid, alcohol, aldehyde and the ester.
3, method according to claim 1 is characterized in that described catalytic reaction can be the unsaturated hydrocarbon selective hydrogenation reaction, the full hydrogenation reaction of unsaturated hydrocarbons; hydroformylation reaction; ammoxidation reaction, oxi-chlorination, olefinic polyreaction or hydrocarbon catalytic cracking reaction.
4, method according to claim 1 is characterized in that described catalytic reaction is the reaction or the C of naphtha, light diesel fuel or catalytic cracking of tar system ethene, propylene
4-C
8Olefin catalytic is preparing propylene transformed, the reaction of ethene.
5, method according to claim 1 is characterized in that described catalytic reaction is C
2-C
5The reaction of unsaturated hydrocarbon selective hydrogenation or full hydrogenation.
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| CN102649717B (en) * | 2011-02-25 | 2014-07-02 | 中国石油化工股份有限公司 | Olefin hydroformylation method |
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| CN104368301B (en) * | 2013-08-14 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of supergravity reactor and reaction method |
| CN103861533B (en) * | 2014-03-21 | 2016-03-02 | 中建安装工程有限公司 | A kind of process units of alkylate oil and production method |
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| CN106178573B (en) * | 2016-08-17 | 2018-09-07 | 浙江工业大学 | Composite rotors is high-gravity rotating bed |
| CN109395667B (en) * | 2017-08-18 | 2021-08-03 | 上海浦景化工技术股份有限公司 | Axial-radial reactor for synthesizing dimethyl oxalate through CO carbonylation coupling |
| CN114478614A (en) * | 2022-03-11 | 2022-05-13 | 新疆晶硕新材料有限公司 | Process and apparatus for the preparation of vinylchlorosilanes |
| CN115368224A (en) * | 2022-08-10 | 2022-11-22 | 北京化工大学 | System device and method for preparing hexamethylene diamine from butadiene |
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|---|---|---|---|---|
| CN1059105A (en) * | 1991-10-08 | 1992-03-04 | 北京化工学院 | Rotating bed super gravity field is strengthened transmission and reaction unit |
| US5254512A (en) * | 1990-11-28 | 1993-10-19 | Sumitomo Seika Chemicals Co., Ltd. | Method for treating gas and regenerating catalyst portion by portion |
| CN1438067A (en) * | 2003-03-06 | 2003-08-27 | 上海交通大学 | Rotary bed super-gravity-field device with new type rotor structure |
| CN1507940A (en) * | 2002-12-16 | 2004-06-30 | 中国石油化工股份有限公司 | Catalytic reaction method |
-
2004
- 2004-09-02 CN CNB2004100736242A patent/CN1327945C/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5254512A (en) * | 1990-11-28 | 1993-10-19 | Sumitomo Seika Chemicals Co., Ltd. | Method for treating gas and regenerating catalyst portion by portion |
| CN1059105A (en) * | 1991-10-08 | 1992-03-04 | 北京化工学院 | Rotating bed super gravity field is strengthened transmission and reaction unit |
| CN1507940A (en) * | 2002-12-16 | 2004-06-30 | 中国石油化工股份有限公司 | Catalytic reaction method |
| CN1438067A (en) * | 2003-03-06 | 2003-08-27 | 上海交通大学 | Rotary bed super-gravity-field device with new type rotor structure |
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