CN106268574A - A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film - Google Patents
A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film Download PDFInfo
- Publication number
- CN106268574A CN106268574A CN201510303219.3A CN201510303219A CN106268574A CN 106268574 A CN106268574 A CN 106268574A CN 201510303219 A CN201510303219 A CN 201510303219A CN 106268574 A CN106268574 A CN 106268574A
- Authority
- CN
- China
- Prior art keywords
- reaction
- liquid film
- bed reactor
- packed bed
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention discloses a kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film.Described method includes: catalyst and filler are loaded in the rotor of rotating packed bed reactor, adds the inert liquid phase medium being not involved in reaction in rotating packed bed reactor；Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter, make the inert liquid phase medium being not involved in reaction form liquid film at catalyst surface；Being passed through vapor-phase reactant, described liquid film selectively allows for vapor-phase reactant and is delivered to catalyst surface carries out catalytic reaction through liquid film.The present invention shows stronger superiority in terms of heat transfer, mass transfer, pressure drop, integer catalyzer active component consumption is less, and can select according to reaction system and have specific selective inert liquid phase solvent and shift a certain reactant, also by changing the rotating speed of rotating packed bed reactor, the regulation and control thickness of liquid film of catalyst surface thus autotelic quantization reaction.
Description
Technical field
The present invention relates to field of catalytic reactions.Realize selecting by regulation and control liquid film more particularly, to one
The property method of catalytic reaction, device and application.
Background technology
Reactor is the main place that chemical reaction occurs.Common reaction have gas-liquid, liquid liquid, gas-solid,
The heterogeneous reactions such as gas-liquid-solid.Wherein, common gas solid reactor type has gas-solid fluidized bed reactor gentle
Gu fixed bed reactors.
Gas-solid fluidized bed reactor structure is relative complex, needs to meet that pressure drop is little, the requirement of high gas velocity in operation,
Process is wayward, therefore requires to compare high with the coupling of reaction system, gas speed in operation, drag-out,
Strict with separation equipment design comparisons such as supporting whirlwind.Using the catalyst of powder, vapour lock is relatively big,
Catalyst loss is serious or disperses unequal rough sledding can affect catalytic effect, and operating condition is improper also
Slug and channel in causing bed.But fluid bed contact area is big, can improve mass transfer environment, space-time produces
Rate is high.Gas-solid-solid fixed bed structure of reactor is simple, it is easy to operation, and reacting fluid is close flat in fixed bed
Plug-flow, with degree for the treatment of difference can disposably or reflux cycle process.It is generally understood that in fixed bed,
Catalyst is fixed, and therefore specific surface area reduces, and its catalytic efficiency decreases.Industry gas-solid reaction anti-
Speed is answered to be about 0.5～15mol/ (m3S), the corresponding rate of heat production is about 0.25～7.5MW/m3.Right
For Fast exothermic reacts, generally by changing catalytic amount, active metal amount, reaction temperature, gas
The parameters such as phase pressure control to move heat.
Either fluid bed or fixed bed, there is also certain drawback and improvement for gas-solid reaction
Space.Especially for the gas solid catalytic reaction of the mixed feeding (A and B) of at least two kinds of components, instead
Answering material A while catalyst surface reacts, the B being not involved in reaction also can occupy catalyst surface sky
Between, therefore can weaken reaction rate, reduce conversion ratio.Such as, ethylene is important industrial chemicals, logical
Petroleum refining industry often can produce the gaseous mixture of ethylene and acetylene.On the one hand, it is desirable to convert the acetylene to ethylene
It is used；Still further aspect, acetylene can make the catalyst poisoning of downstream vinyl polymerization.At catalyst
Under effect, it is desirable to the acetylene in gaseous mixture (ethylene and acetylene) is carried out selective hydrogenation, maximum
Limit convert the acetylene to ethylene.But during real reaction, ethylene molecule and acetylene molecule all can occupy and urge
Agent surface, reduces the probability that acetylene molecule contacts with catalyst.
It is bullied the inspiration of liquid-solid reaction, if inert third phase (liquid phase) can be introduced in gas solid reactor,
Realize the covering liquid film at the catalyst surface selectivity transmittance process to gaseous mixture, finally realize gas-solid anti-
The selective catalysis reaction answered.The shifting heat of reaction is not only had an impact by the thickness of liquid film, affects gas phase simultaneously
Left the mass transfer being diffused into gas phase main body from catalyst surface by Liquid film diffusion to catalyst surface, product
Resistance.But the fixed bed reactors of routine, the general thickness being difficult to regulation and control catalyst liquid film, to realize passing
The regulation and control of matter resistance.
Summary of the invention
First purpose of the present invention is that providing a kind of realizes selective catalysis reaction by regulation and control liquid film
Method.
It is anti-that second object of the present invention is to provide a kind of enforcement to realize selective catalysis by regulation and control liquid film
The device of induction method.
It is anti-that third object of the present invention is to provide a kind of enforcement to realize selective catalysis by regulation and control liquid film
The application of the device of induction method.
Rotating packed bed reactor has mass transfer and the microcosmic mixed performance of excellence.High-gravity rotating bed
In reactor, the regulation and control to thickness of liquid film can be realized by regulation and control revolving bed rotating speed.Simultaneously as liquid
Film has quick renewal frequency in rotary drill reactor, is advantageous to product and speeds away catalyst
Surface, it is achieved efficient catalytic separates with product.Therefore the present invention proposes a kind of in high-gravity rotating bed reaction
Device introduces third phase, it is achieved the method for gas-solid selective catalysis reaction.
Catalyst is loaded in rotor, makes gas-solid reaction carry out in rotating packed bed reactor.?
Add certain inert liquid phase medium in rotating packed bed reactor, regulate rotating bed reaction by converter
Device rotating speed regulates and controls the thickness of liquid film of filling surface liquid phase, thus regulates and controls the mass transfer rate of gas phase or produce thing
Diffusion rate.Described liquid film has certain selectivity to gas, and some specific gas phase optional is anti-
Answer thing to be delivered to Gas-solid surface and participate in catalytic reaction.
For reaching above-mentioned first purpose, the present invention uses following technical proposals:
A kind of method realizing selective catalysis reaction by regulation and control liquid film, comprises the steps:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
Being passed through vapor-phase reactant, described liquid film selectively allows for vapor-phase reactant and penetrates liquid film and be delivered to urge
Agent surface carries out catalytic reaction.
Technical solution of the present invention needs to find the inert liquid phase medium of suitable reaction system, needs reactant
And the character of product has careful deep understanding.Different reactant character has the biggest difference, needs root
According to its character such as polarity, dissolubility, inert liquid phase medium is selected.Selected liquid phase medium should not be joined
Add target response, catalyst activity component should not had dissolving or toxic action, and in reaction temperature and pressure
Do not undergo phase transition under power.
Preferably, the inert liquid phase medium of reaction it is not involved in described in selected from having the solvent of polarity, supercritical
One or more in fluid and ionic liquid.
Preferably, when the rotating speed of rotating packed bed reactor is 50～2400rpm, and the thickness of liquid film is
10～50 μm.
It is highly preferred that when the rotating speed of rotating packed bed reactor is 500～1500rpm, the thickness of liquid film
It is 17～27 μm.
What technical solution of the present invention also needed to solve one technical problem is that greatly fixing on carrier of catalyst is asked
Topic, especially when the rotating speed of revolving bed is the highest, has the highest to the adhesion between active component and carrier
Requirement.
Therefore, for solving above-mentioned technical problem, the present invention uses following technical proposals:
A kind of device implementing to realize selective catalysis reaction method as described above by regulation and control liquid film, described
Device is rotating packed bed reactor, loading catalyst in the rotor of described rotating packed bed reactor
With filler, described catalyst and filler are the catalyst filling of Integral-structure type, described Integral-structure type
Catalyst filling includes basic framework and active component.
Preferably, fluid in reactor was both cut by described basic framework, can support again Second support,
Active component and promoter etc., need to possess certain mechanical strength.Described basic framework is filling out of monoblock
Material, or the concentric insertion ring that diameter is different.
Preferably, described active component has been the essence material of catalytic action, can be precious metal simple substance
Pt, Pu, Ru etc., precious metal chemical complex CuO, PdCl2Deng, base metal Cu, Fe, Mn etc.,
Or non-noble metal compound dimethylamino pyridine, 4-pyrrolidine pyridine, triphenylphosphine etc..
Preferably, the material of described basic framework be kieselguhr, cordierite, meerschaum, foamed ceramics,
Foam metal, foamed alloy or metal gauze etc..
Preferably, the catalyst filling of described Integral-structure type also includes Second support and promoter.
Preferably, described Second support needs possess certain specific surface area, for Al2O3、CeO2-Y2O3
Or LaAlO3Deng.
Preferably, described promoter can improve the activity and selectivity of major catalyst, improves catalyst resistance to
Hot and life-spans etc., in Li, Na, K, Mg, Ca, Mo, Sr, Ba, La, Ce and Zr
One or more etc..
For reaching above-mentioned 3rd purpose, the invention also discloses device as above by regulation and control liquid
Film realizes the application in the gas-liquid-solid phase reaction of selective catalysis reaction.
Beneficial effects of the present invention is as follows:
(1) heat transfer aspect, filler is according to overall structure, and owing to its duct is many, hole wall is relatively thin, compares table
Area is high, can remove, by large-area liquid film, the heat that reaction produces, prevent reaction temperature suddenly
Raise；
(2) mass transfer aspect, uses the Integral-structure type catalyst of coating type, and active component is dispersed in surface
On, high specific surface area shortens reactant and arrives the diffusion path in active center；Meanwhile, at centrifugal force
Under effect, the filled continuous shearing of liquid film, accelerate renewal frequency；
(3) pressure drop aspect, the outstanding feature of integer catalyzer is exactly that pressure drop is low, and its hole path decreases stream
Dynamic resistance, low 2-3 the order of magnitude of its pressure drop ratio pellet type catalyst when identical air speed；
(4) integer catalyzer active component consumption is less, typically not over 30%；
(5) selectivity aspect, can select according to reaction system and have specific selective inert liquid phase solvent
Shift a certain reactant, also by the rotating speed of change rotating packed bed reactor, regulate and control catalyst
The thickness of liquid film on surface thus autotelic quantization reaction.
Accompanying drawing explanation
Below in conjunction with the accompanying drawings the detailed description of the invention of the present invention is described in further detail.
Fig. 1 illustrates that rotating packed bed reactor of the present invention carries out gas-solid reaction flow chart.
Detailed description of the invention
In order to be illustrated more clearly that the present invention, below in conjunction with preferred embodiments and drawings, the present invention is done into one
The explanation of step.Parts similar in accompanying drawing are indicated with identical reference.Those skilled in the art
Should be appreciated that following specifically described content is illustrative and be not restrictive, should not limit with this
Protection scope of the present invention.
Fig. 1 illustrates that rotating packed bed reactor of the present invention carries out gas-solid reaction flow chart.Each several part in figure
The implication represented is: 1,2-unstripped gas steel cylinder；3-pressure-regulating valve；4-mass flowmenter；5-main valve；6-
Check-valves；7-rotating packed bed reactor (RPB)；8-counterbalance valve；9-cooler；10-liquid phase samples
Pipe；11-gas-liquid separator；12-counterbalance valve；13-mass flowmenter；14-ball valve；15 storage tanks；16-pump.
As shown in Figure 1: the unstripped gas of purification is from unstripped gas steel cylinder 1,2 through pressure-regulating valve 3 level pressure extremely
Pressure needed for response system, enters reactor by mass flowmenter 4, simultaneously with micro-after then being measured
Liquid phase (supercritical fluid or ionic liquid etc.) medium is squeezed in rotating packed bed reactor 7 by amount pump,
Make reaction mass mix homogeneously in rotating packed bed reactor, and use artificial intelligence system accurately to control
Temperature.By gas-liquid separator separates after the cooling of gas condensed device after reaction.
Embodiment 1
The devices such as pyrolysis device residual C4 fraction, catalytic cracking (FCC) and steam cracking are produced on a small quantity
Butadiene is processed further utilization to C 4 fraction the biggest obstruction, uses selection hydrogenation to remove butadiene and is
Economically viable way.
The method realizing selecting hydrogenation to remove butadiene by regulation and control liquid film comprises the steps:
Integer catalyzer is seated in the rotor of rotating packed bed reactor (RPB), to hypergravity
Rotary drill reactor adds the inert liquid phase medium being not involved in reaction；In described gravity rotary drill reactor
Catalyst basic framework be foamed aluminium, foamed aluminium surface applications anodised method coating last layer
γ-Al2O3As Second support, active component be Ni, Mo be promoter.Inert liquid phase medium uses
Imidazolium ionic liquid 1-fourth with N-Methylimidazole., bromination of n-butane, sodium tetrafluoroborate as Material synthesis
Base-3-methyl imidazolium tetrafluoroborate ([bmim] BF4)；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
Being passed through vapor-phase reactant, described liquid film selectively allows for vapor-phase reactant and is delivered to urge through liquid film
Agent surface carries out catalytic reaction；Process conditions: reaction temperature 160 DEG C, reaction pressure 2.2MPa, instead
Sampling is started after answering 48 hours.
Integer catalyzer filling surface [bmim] BF is regulated and controled by changing high-gravity rotating bed rotating speed4Liquid film
Thickness, the amount of the butadiene wherein dissolved changes therewith, such that it is able to selectively manipulation react into
The degree of row.Investigating the impact on hydrogenation degree of the different RPB rotating speed, result is as shown in table 1.Along with RPB
The raising of rotating speed, the butadiene in raw material can remove substantially completely, but monoolefine is also hydrogenated saturated,
Butane content dramatically increases, and therefore needs to select suitable RPB rotating speed.
The impact that butadiene hydrogenation is reacted by the different RPB rotating speed of table 1
| RPB rotating speed/rpm | Thickness of liquid film/μm | W (butane)/% | W (butylene)/% | W (butadiene)/% |
| 400 | 26.2 | 4.97 | 90.16 | 2.91 |
| 800 | 20.5 | 5.07 | 90.54 | 2.43 |
| 1200 | 18.2 | 6.86 | 89.21 | 1.97 |
| 1600 | 17.9 | 7.74 | 89.17 | 0.53 |
| 2000 | 17.4 | 8.01 | 88.93 | 0.21 |
Embodiment 2
Ethylene and acetylene gaseous mixture selective hydrogenation, realized second to greatest extent by regulation and control liquid film
Alkynes is converted into the method for ethylene, comprises the steps:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；Entirety in described gravity rotary drill reactor
The basic framework of catalyst is foam α-Al2O3, the Palladous chloride. of load is active component, introduces inertia liquid phase
Medium N-Methyl pyrrolidone (NMP) is as third phase, anti-to form the hydrogenation of gas-liquid-solid three-phase existence
Should；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
Being passed through vapor-phase reactant, described liquid film selectively allows for vapor-phase reactant and is delivered to urge through liquid film
Agent surface carries out catalytic reaction；Reaction condition is: normal pressure, and temperature is 160 DEG C, and reaction gas is H2(99.99%)
And C2H2(99.99%) gaseous mixture, hydrogen alkynes mol ratio is n (H2):n(C2H2)=1.
Under the above-described reaction conditions, high-gravity rotating bed rotating speed is to conversion of alkyne, ethylene selectivity, second
The affecting laws of alkene yield, result is as shown in table 2.Along with the raising of RPB rotating speed, conversion of alkyne increases
Greatly.
The impact on acetylene selective hydrogenation synthesizing ethylene product of the table 2 RPB rotating speed
| RPB rotating speed/rpm | Thickness of liquid film/μm | XC2H2(%) | SC2H4(%) | YC2H4(%) |
| 1600 | 17.9 | 81.7 | 91.8 | 75.0 |
| 1200 | 18.2 | 52.5 | 92.3 | 48.5 |
| 800 | 20.5 | 25.7 | 90.9 | 23.4 |
| 400 | 26.2 | 15.4 | 96.3 | 14.8 |
Embodiment 3
The method realizing synthesis gas synthesizing methanol by regulation and control liquid film, comprises the steps:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；Described gravity rotary drill reactor use negative
Load type C302-2 type copper-based catalysts, active component is CuO, and basic framework is stainless steel cloth；Inertia
Liquid phase medium is normal hexane supercritical medium；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
It is passed through vapor-phase reactant, reaction condition: temperature 235～260 DEG C, gaseous mass air speed 450～1600L
(STP)·(kg cat)-1·h-1, react stagnation pressure 6.0～7.0MPa, dividing potential drop shared by unstripped gas is 3.0～3.7MPa,
Supercritical medium dividing potential drop 3.0～3.4MPa.Fixing RPB rotating speed is 1500rpm, and thickness of liquid film now is about
It is 17.4 μm.Unstripped gas composition is as follows: supercritical RPB reaction experiment with No. 1 unstripped gas CO 9.06%,
CO24.524%, H248.155%, N238.274%；The reaction experiment of RPB without supercritical is with No. 2 raw materials
Gas CO 9.273%, CO24.592%, H251.871%, N234.267%.Experimental data such as table 3
And shown in table 4, numbering 1-1～1-5's is based on reactor outlet thing under the conditions of No. 1 unstripped gas different operating
Matter composition, numbering 2-1～2-5's is based on reactor outlet material group under the conditions of No. 2 unstripped gas different operatings
Become.It can be seen that do not introduce the CO conversion ratio of the RPB methanol-fueled CLC of inert liquid phase medium and methanol goes out
Mouth concentration is corresponding CO equilibrium conversion and methanol outlet equilibrium concentration less than under its operating condition, and draws
Enter inert liquid phase medium liquid paraffin and normal hexane supercritical medium carries out RPB methanol under supercriticality and closes
The CO conversion ratio and the methanol outlet concentration that become reaction are all substantially high in addition to the experimental point 1-5 of sequence number 5 correspondence
In its equilibrium valve, this shows that the n-hexane being under super critical condition serves the work of Reaction Separation-coupling
With, displaced the thermodynamical equilibrium restriction to CO conversion per pass, thus it is anti-to drastically increase RPB
Device is answered to export Methanol Molar mark.
Methanol-fueled CLC experimental data in table 3 inert liquid phase medium
Table 4 is without methanol-fueled CLC experimental data under the conditions of liquid phase medium
Embodiment 4
By regulation and control liquid film realize selective catalysis synthesizing methanol, isobutanol method, including walking as follows
Rapid:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；Described gravity rotary drill reactor is selected and lives
Property component be that Zr-Mn-K composite catalyst adsorption precipitation method is supported on overall tripolite filling material, inertia
(mean molecule quantity is 168 to the mixture of liquid phase medium selection supercritical medium C11～C13 N-alkanes, connects
The molecular weight 170 of nearly dodecane, the critical temperature of n-dodecane is 385 DEG C, and critical pressure is 1.81MPa)；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
Being passed through vapor-phase reactant, reaction condition is: reaction temperature 360～410 DEG C, synthesis gas pressure 7.5MPa,
GHSV1700h-1And pressure medium be 2.08MPa, RPB rotating speed be 1200rpm, now thickness of liquid film is
18.2 μm, the products distribution obtained such as table 5.And under the conditions of supercritical phase catalyzes and synthesizes, by changing
RPB rotating speed changes thickness and the flow regime of integer catalyzer filling surface liquid film, investigates products distribution
With the change of RPB rotating speed, result such as table 6.
The distribution of alcohol in table 5 product
| ROH forms (%) | MeOH | EtOH | n-PrOH | i-BuOH | i-PnOH | HOH |
| Simple gas phase reaction | 85.92 | 0.23 | 0.54 | 11.27 | 0.31 | 0.38 |
| Supercritical phase reaction | 43.7 | 19.59 | 8.1 | 12.38 | 3.39 | 12.81 |
As can be seen from Table 5, supercritical phase reaction for the selectivity of methanol and isobutanol apparently higher than list
Pure gas phase, illustrates that supercritical fluid promotes desorption and the transmission of product, improves the conversion ratio of CO.
Table 6 RPB rotating speed is on the impact of alcohol distribution in product
As can be seen from Table 6, along with RPB rotating speed changes, product composition also can occur to change accordingly.
When under this experiment condition, rotating speed is 1200rpm, products distribution is more excellent.
Embodiment 5
The method realizing selective catalysis alkane and the direct oxonation of CO by regulation and control liquid film, including
Following steps:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；Select ionic liquid at room temperature chlorination 1-methyl-3-
Ethyl imidazol(e) ionic liquid (MEImCl), chloridization 1-methyl-3-butyl pyridine ion liquid (MBImCl)
With chlorination 1-butyl-pyridinium (BpyCl) as inert liquid phase medium, in described gravity rotary drill reactor
The active component of catalyst is aluminum chloride, the γ-Al being supported on integral foam aluminum2O3Coating (Second support)
On.
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
Order is not involved in the inert liquid phase medium of reaction and forms liquid film at catalyst surface, and the rotating speed controlling RPB is
1200, now the thickness of liquid film is 18.4 μm.
Being passed through vapor-phase reactant pure isooctane, described liquid film selectively allows for vapor-phase reactant and wears
Transparent liquid film is delivered to catalyst surface and carries out catalytic reaction；Reaction condition is: under HCl atmosphere, reaction temperature
Degree is 130 DEG C, and reaction pressure is 5.0MPa, reacts 6h.
The reaction result of Alkane Carbonylation is listed in table 7.As can be seen from the table, ionic liquid is different, and carbonylation produces
Thing distribution is also different.There is in MEImCl higher conversion ratio, but the distribution of product is average；
In BpyCl, conversion ratio is the lowest, but tert-butyl group isobutenyl ketone has at a relatively high selectivity, shows sun
Reaction is had a certain impact by ionic portions.Can draw, can be by selecting different types of ionic liquid
Body regulates and controls the products distribution in RPB.
Alkane Carbonylation result in table 7 superpower acidity ionic liquid at room temperature
Obviously, the above embodiment of the present invention is only for clearly demonstrating example of the present invention, and
It is not the restriction to embodiments of the present invention, for those of ordinary skill in the field,
Can also make other changes in different forms on the basis of described above, here cannot be to all
Embodiment give exhaustive, every belong to the obvious change that technical scheme extended out
Change or change the row still in protection scope of the present invention.
Claims (10)
1. one kind by regulation and control liquid film realize selective catalysis reaction method, it is characterised in that include as
Lower step:
Catalyst and filler are loaded in the rotor of rotating packed bed reactor, to high-gravity rotating bed
Reactor adds the inert liquid phase medium being not involved in reaction；
Open rotating packed bed reactor, regulate rotating packed bed reactor rotating speed by converter,
The inert liquid phase medium being not involved in reaction is made to form liquid film at catalyst surface；
Being passed through vapor-phase reactant, described liquid film selectively allows for vapor-phase reactant and is delivered to urge through liquid film
Agent surface carries out catalytic reaction.
A kind of method realizing selective catalysis reaction by regulation and control liquid film the most according to claim 1,
It is characterized in that: described in be not involved in the inert liquid phase medium of reaction selected from having the solvent of polarity, supercritical
One or more in fluid and ionic liquid.
A kind of method realizing selective catalysis reaction by regulation and control liquid film the most according to claim 1,
It is characterized in that: when the rotating speed of rotating packed bed reactor is 50～2400rpm, and the thickness of liquid film is
10～50 μm.
A kind of method realizing selective catalysis reaction by regulation and control liquid film the most according to claim 1,
It is characterized in that: preferably, when the rotating speed of rotating packed bed reactor is 500～1500rpm, liquid film
Thickness be 17～27 μm.
5. implement to realize selective catalysis reaction by regulation and control liquid film as described in claim 1-4 is arbitrary for one kind
The device of method, described device is rotating packed bed reactor, it is characterised in that: described hypergravity revolves
Loading catalyst and filler in the rotor of rotated bed reactor, described catalyst and filler are Integral-structure type
Catalyst filling, the catalyst filling of described Integral-structure type includes basic framework and active component.
Device the most according to claim 5, it is characterised in that: described basic framework is filling out of monoblock
Material, or the concentric insertion ring that diameter is different；The material of described basic framework be kieselguhr, cordierite,
Meerschaum, foamed ceramics, foam metal, foamed alloy or metal gauze.
Device the most according to claim 5, it is characterised in that: described active component is noble metal list
Matter, precious metal chemical complex, base metal simple substance or non-noble metal compound.
Device the most according to claim 5, it is characterised in that: the catalyst of described Integral-structure type
Filler also includes Second support and promoter.
Device the most according to claim 8, it is characterised in that: described Second support is Al2O3、
CeO2-Y2O3, or LaAlO3；Described promoter selected from Li, Na, K, Mg, Ca, Mo, Sr,
One or more in Ba, La, Ce and Zr.
10. device as claimed in claim 5 is realizing the gas of selective catalysis reaction by regulation and control liquid film
Application in liquid-solid phase reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510303219.3A CN106268574A (en) | 2015-06-04 | 2015-06-04 | A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510303219.3A CN106268574A (en) | 2015-06-04 | 2015-06-04 | A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106268574A true CN106268574A (en) | 2017-01-04 |
Family
ID=57656682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510303219.3A Pending CN106268574A (en) | 2015-06-04 | 2015-06-04 | A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106268574A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111072494A (en) * | 2019-12-26 | 2020-04-28 | 湖北吉和昌化工科技有限公司 | Preparation method of N, N-diethyl propargylamine |
| CN111468065A (en) * | 2020-04-24 | 2020-07-31 | 烟台大学 | Production device and production process of high-activity polyisobutylene |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1446786A (en) * | 2003-03-14 | 2003-10-08 | 华东理工大学 | Method and equips for manufacturing dimethyl ether with synthesis gas as raw material by using circulating current bed |
| CN103012624A (en) * | 2011-09-20 | 2013-04-03 | 中国石油天然气股份有限公司 | Spherical magnesium halide catalyst carrier, preparation and applications thereof |
| JP2013226554A (en) * | 2013-06-05 | 2013-11-07 | Mitsubishi Chemicals Corp | Plate-type reactor, method for producing reaction product by using the same, and method for packing catalyst |
| CN104073307A (en) * | 2014-07-08 | 2014-10-01 | 赛鼎工程有限公司 | Sulfur methanation resistant process for preparing substitute natural gas from coke-oven gas |
| CN104073308A (en) * | 2014-07-08 | 2014-10-01 | 赛鼎工程有限公司 | Sulfur methanation resistant process for preparing substitute natural gas from synthetic gas |
| CN104549100A (en) * | 2013-10-16 | 2015-04-29 | 北京化工大学 | Novel passive super-gravity rotary bed device |
-
2015
- 2015-06-04 CN CN201510303219.3A patent/CN106268574A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1446786A (en) * | 2003-03-14 | 2003-10-08 | 华东理工大学 | Method and equips for manufacturing dimethyl ether with synthesis gas as raw material by using circulating current bed |
| CN103012624A (en) * | 2011-09-20 | 2013-04-03 | 中国石油天然气股份有限公司 | Spherical magnesium halide catalyst carrier, preparation and applications thereof |
| JP2013226554A (en) * | 2013-06-05 | 2013-11-07 | Mitsubishi Chemicals Corp | Plate-type reactor, method for producing reaction product by using the same, and method for packing catalyst |
| CN104549100A (en) * | 2013-10-16 | 2015-04-29 | 北京化工大学 | Novel passive super-gravity rotary bed device |
| CN104073307A (en) * | 2014-07-08 | 2014-10-01 | 赛鼎工程有限公司 | Sulfur methanation resistant process for preparing substitute natural gas from coke-oven gas |
| CN104073308A (en) * | 2014-07-08 | 2014-10-01 | 赛鼎工程有限公司 | Sulfur methanation resistant process for preparing substitute natural gas from synthetic gas |
Non-Patent Citations (1)
| Title |
|---|
| 李京刚等: "超临界条件下甲醇合成的气液传质系数测定", 《化工学报》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111072494A (en) * | 2019-12-26 | 2020-04-28 | 湖北吉和昌化工科技有限公司 | Preparation method of N, N-diethyl propargylamine |
| CN111072494B (en) * | 2019-12-26 | 2022-12-06 | 湖北吉和昌化工科技有限公司 | Preparation method of N, N-diethyl propargylamine |
| CN111468065A (en) * | 2020-04-24 | 2020-07-31 | 烟台大学 | Production device and production process of high-activity polyisobutylene |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108620092B (en) | Alumina-supported PtCu monatomic alloy catalyst and preparation method and application thereof | |
| CN111408370B (en) | Supported PtZn intermetallic alloy catalyst and preparation method and application thereof | |
| CN102206130B (en) | Selective hydrogenation method of C2 fraction | |
| CN100417436C (en) | Catalytic selective hydrogenation | |
| CN102746087B (en) | Method for preparing cyclohexane by catalyzing and hydrogenising benzene at room temperature | |
| CN105017317B (en) | A method of the alkene two-phase hydroformylation based on phosphine functionalization polyethers ionic liquid of alkyl guanidine salt | |
| CN107185594A (en) | A kind of preparation method of Ni Zn K Ru/MOF catalyst | |
| CN102256700B (en) | Selective catalytic hydrogenation of alkynes to corresponding alkenes | |
| CN109701552A (en) | A kind of palladium-copper system support type sub-nanometer catalyst and preparation method thereof | |
| CN107879907A (en) | A kind of high selectivity Oxidation Ethylbenzene acetophenone technique | |
| CN104415715A (en) | Catalytic hydrogenation method | |
| US9850184B2 (en) | Triphasic flow millireactors | |
| CN106268574A (en) | A kind of method, device and application being realized selective catalysis reaction by regulation and control liquid film | |
| CN102220168A (en) | Method for selective hydrogenation of pyrolysis gas | |
| CN1120047C (en) | Catalyst for preparing propylene by dismutation reaction and its preparing process and application | |
| CN105732261A (en) | Selective hydrogenation method of trace amount of acetylene in methanol-to-olefin apparatus | |
| CN105732281A (en) | Front-depropanization front-hydrogenation method for C2 fraction | |
| CN106478352A (en) | A kind of method producing high-purity isobutylene | |
| CN105732274A (en) | Method of purifying ethylene through selective hydrogenation | |
| CN108499559A (en) | A kind of catalyst for preparing isobutene through dehydrogenation of iso-butane, preparation method and application | |
| CN105732276A (en) | Front-deethanization front-hydrogenation method for C2 fraction | |
| CN105732271A (en) | Front-hydrogenation method of trace amount of acetylene in methanol to olefin (MTO) apparatus | |
| CN105732267A (en) | Selective hydrogenation method for C2 fraction | |
| CN107880217B (en) | Method and device for processing butane | |
| CN101234352A (en) | Catalyst based on second metal of different group VIII of platinum and iridium used for opening ring compounds |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170104 |
|
| RJ01 | Rejection of invention patent application after publication |