CN108380141A - Bubbling bed reactor, methyl methacrylate production equipment - Google Patents
Bubbling bed reactor, methyl methacrylate production equipment Download PDFInfo
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- CN108380141A CN108380141A CN201810218237.5A CN201810218237A CN108380141A CN 108380141 A CN108380141 A CN 108380141A CN 201810218237 A CN201810218237 A CN 201810218237A CN 108380141 A CN108380141 A CN 108380141A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/39—Preparation of carboxylic acid esters by oxidation of groups which are precursors for the acid moiety of the ester
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/006—Separating solid material from the gas/liquid stream by filtration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/007—Separating solid material from the gas/liquid stream by sedimentation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
- C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00123—Fingers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This application discloses a kind of bubbling bed synthesis reactor.The reactor includes catalyst reaction section and catalyst sedimentation section, and the cross-sectional area of at least one position of the catalyst reaction section is less than the cross-sectional area of at least one position of the catalyst sedimentation section；The catalyst reaction section is located at the lower section of the catalyst sedimentation section.The reactor realizes the high conversion, highly selective for the reaction system easily polymerizeing for strongly exothermic, product, has compared with existing such industrialization technology and once invests low, the low competitive advantage of production cost.Disclosed herein as well is a kind of equipment producing methyl methacrylate.
Description
Technical field
This application involves a kind of bubbling bed reactors, belong to field of chemical engineering.
Background technology
In traditional methyl methacrylate synthesis process, majority using multiple concatenated bands stirrings, (or stir by multistage
Mix) and cooling jacket reaction kettle as being aoxidized under the action of catalyst as raw material using methacrolein, methanol, containing oxygen gas mixture
Esterification, although the industrialized production of methyl methacrylate can be realized, since the oxidative esterification of methacrolein is anti-
Should be strong exothermal reaction (reaction heat is about 300KJ/mol), and raw material methacrolein and product methyl methacrylate appearance
Easily polymerization, the other inherent defect of reaction kettle, if raw material, catalyst and oxygen disperse uneven, mass transfer effect is poor, heat transfer efficiency
It is low, and side reaction is more, and reaction heat is difficult to remove, and causes product purifying technique complicated, long flow path, product quality is not easy surely
The restraining factors such as fixed.
Invention content
According to the one side of the application, provide a kind of reactor, the reactor realize simultaneously raw material, catalyst,
High degree of dispersion is uniform in the reactor for oxygen, and mass transfer effect is superior, moves the high technological requirement of the thermal efficiency.The reactor can be applicable in
In the process of aldehydes or the oxidative esterification reaction of alcohols, especially methyl methacrylate synthetic reaction process.
The bubbling bed reactor, which is characterized in that the reactor includes catalyst reaction section and catalyst sedimentation section；
The cross-sectional area of at least one position of the catalyst reaction section is less than at least one of the catalyst sedimentation section
The cross-sectional area of position；
The catalyst reaction section is located at the lower section of the catalyst sedimentation section.
Optionally, the cross-sectional area of the catalyst reaction section any position is less than any position of the catalyst sedimentation section
Cross-sectional area；
The catalyst reaction section and catalyst sedimentation section are coaxially connected.
Optionally, the length of the catalyst sedimentation section is less than the length of the catalyst reaction section.
The diameter range of the catalyst reaction section is 20~10000mm, and length range is 100~50000mm；
The diameter of the catalyst sedimentation section is 1.2~3.0 times of catalyst reaction section diameter, and length is that catalyst reaction section is long
The 0.1~0.8 of degree.
Optionally, the diameter range of the catalyst reaction section of the reactor be 50~5000mm, length range be 300~
30000mm。
Optionally, the diameter of the catalyst sedimentation section of the reactor is 1.5~2.0 times of catalyst reaction section, and length is
The 0.2~0.6 of catalyst reaction section.There is liquid to produce filter element in the catalyst sedimentation section.
Optionally, 20~10000mm of diameter range of the catalyst reaction section of the reactor, length range 100~
Setting takes thermal, gas distributor and gas-liquid distributor in 50000mm.
Optionally, include taking thermal, gas distributor and gas-liquid distributor in the catalyst reaction section；The catalyst
Settling section includes liquid extraction filter element.
Optionally, the catalyst reaction section includes catalyst reaction section cylinder, takes thermal, gas-liquid distributor, gas distribution
Device；Wherein, described that thermal, gas-liquid distributor and gas distributor is taken to be located in catalyst reaction section cylinder；
The catalyst sedimentation section includes catalyst sedimentation section cylinder, filter element；Wherein, the filter element is located at and urges
In agent settling section cylinder.
The catalyst reaction section cylinder and catalyst sedimentation section cylinder coaxial communication；The diameter of the catalyst reaction section cylinder
Less than the diameter of catalyst sedimentation section cylinder.
Optionally, the bubbling bed reactor is gas, liquid, solid three-phase bubbling bed MMA synthesis reactor；The reactor packet
Catalyst reaction section and catalyst sedimentation section are included, cooling device, gas-liquid distributor, gas distributor etc. are set in catalyst reaction section；
Setting liquid produces element kit etc. in catalyst sedimentation section.
Optionally, described includes two sections of cylinders of catalyst reaction section and catalyst sedimentation section；Setting in catalyst reaction section cylinder
By gas distributor (connected and formed with branch pipe and distribution cap by distribution supervisor), gas-liquid distributor (by distribution grid and several distributions
Device unit forms), take setting liquid in thermal (multiple that hot cell is taken to compose in parallel), catalyst sedimentation section cylinder to produce filtering
Unit (is composed in parallel) by multigroup filter.
It is optionally, described that take thermal include at least one set of taking going out for hot cell, the intake header of coolant liquid and coolant liquid
Mouth manifold；
Wherein, the outlet header of the intake header for taking hot cell and coolant liquid and coolant liquid connects；
The intake header of the coolant liquid and the outlet header of coolant liquid are located at the top of the catalyst reaction section cylinder；
The intake header of the coolant liquid the import of reactor, the coolant liquid outlet header in the outlet of reactor
It is respectively positioned on the outer wall of the catalyst reaction section cylinder.
Optionally, described to take the operation medium of thermal for coolant liquid, coolant liquid selects water, brine, glycol water
At least one of, the operation medium in the cylinder includes material solution, catalyst solid particle, nitrogen oxygen atmosphere and reaction
Product.In methyl methacrylate synthetic system, reaction product is methyl methacrylate.
It is described to take cooling of the thermal for reactor, it is quickly reduced phlegm and internal heat by taking thermal coolant liquid with realizing, Jin Erti
The selectivity of high product.
Optionally, described that thermal is taken to pass in and out the manifold of reactor by coolant liquid and multigroup hot cell is taken to compose in parallel.
Optionally, it includes a down-comer and at least one tedge that described one group, which takes hot cell,；
The lower part of the tedge is connect with down-comer, rounded to be uniformly distributed；The tedge converges to be formed in push pipe
One outlet pipe, exit duct diameter are identical as pipe diameter is declined；
Wherein, the down-comer is connect with the intake header of the coolant liquid；The tedge goes out with the coolant liquid
Mouth manifold connections.
Every group takes hot cell to be made of a down-comer and several tedges.
It is described that hot cell effect is taken to be to increase cooling liquid speed, strengthen and move except the thermal efficiency, also spallation reaction device cylinder
The rising bubbling polymerization of internal oxygenous gaseous mixture improves the effect of reaction efficiency at the effect of air pocket.
The cooling liquid inlet and cooling liquid outlet are located on the outer wall of reactor shell；The intake header of coolant liquid and go out
On the top of cylinder, coolant liquid is entered each decline for taking hot cell mounted on inner barrel by import for mouth manifold settings
Pipe, and have the function that cooling reaction system back to cooling liquid outlet manifold outflows after its tedge fluid interchange.
Optionally, the diameter range of the down-comer is 10-200mm；
The quantity of the tedge is at 1-10；
The a diameter of 1/8-1/2 for declining pipe diameter of the tedge.
Optionally, the diameter range of the down-comer is 20-100mm.
Optionally, the diameter upper limit of the down-comer is selected from 20mm, 25mm, 40mm, 100mm, 200mm；Lower limit is selected from
10mm、20mm、25mm、40mm、100mm。
Optionally, the quantity of tedge is at 2-6, and lower part is connect with down-comer, rounded uniformly distributed, under tedge is a diameter of
The 1/6~1/4 of pipe diameter drops, and tedge converges to form one outlet pipe in push pipe, and exit duct diameter is identical as pipe diameter is declined；
200~6000mm of length range of hot cell is taken, it can be by module, single group or multigroup mounted on inside reactor.
Optionally, described to take hot cell be by module, single group or multigroup mounted on inside reactor.
Optionally, it is parallel connection that at least one set, which takes hot cell,；
It is described to take the length of hot cell for 100~10000mm；
It is described that hot cell is taken to be vertically positioned in the catalyst reaction section cylinder, it is uniformly distributed by square, it respectively takes between hot cell
Spacing be 20-2000mm.
Optionally, the length limit for taking hot cell is selected from 800mm, 10000mm；Lower limit is selected from 100mm, 800mm.
Optionally, described respectively to take the spacing of hot cell for 50-1000mm.Such as 50mm, 100mm, 200mm, 300mm,
Arbitrary point value in the range that any two forms in 400mm, 500mm, 600mm and the above point value.It respectively takes between hot cell
Spacing equal can not also wait, under preferable case, respectively take the spacing between hot cell equal.
Optionally, the gas-liquid distributor includes distribution grid and distribution cap；It is anti-that the gas-liquid distributor is located at the catalysis
Answer the bottom of section cylinder.
The working mechanism of the distributor：
Gas-liquid mixture high degree of dispersion is realized using the high-ratio surface microvia interface effect of distribution cap and forms Uniform jet,
It keeps catalyst granules to suspend and realizes high efficiency mass transfer and the heat transfer of material mixed gas liquid and catalyst granules in the reactor.
Optionally, for the average pore size on the distribution grid between 1~50 μm, percent opening is 0.01%~2.0%；
The quantity of the distribution cap is 10-5000；
A diameter of 5-100mm of the distribution cap, length or height are 5-100mm；
The distribution cap is hollow cylinder or cone；
Arrangement mode of the distribution cap on distribution grid is selected from least one of equilateral triangle, square, between arrangement
Away from for 15~200mm.
Optionally, the distribution cap is added by at least one of sintered metal wire-mesh, sintered metal powder, ceramic junction powder
Hollow cylinder or cone made of work.
Optionally, the upper limit of the average pore size on the distribution grid is selected from 20 μm, 50 μm；Lower limit is selected from 1 μm, 20 μm.
Optionally, the percent opening upper limit on the distribution grid is selected from 0.05%, 2.0%；Lower limit be selected from 0.01%,
0.05%.Optionally, gas-liquid distributor is arranged in the catalyst reaction section bottom of the reactor, by distribution grid and distribution cap；
Optionally, the upper average pore size on the distribution grid is between 5~20 μm, and percent opening is 0.02%~1.5%
Between；The quantity of the distribution cap is 20-1000.
Optionally, a diameter of 10-50mm of the distribution cap, length or height are 20-50mm, and the distribution cap is being distributed
Arrangement mode on plate is selected from least one of equilateral triangle, square, and its spacing is 40~100mm.
Optionally, gas distributor is arranged in the catalyst reaction section bottom of the reactor, acts on mixture of feed body
Uniform gas-liquid mixture is formed with feed liquid.
Optionally, the gas distributor include distributor supervisor and distributor branch pipes, each distributor branch pipes with described point
The supervisor of cloth device is connected；
The gas distributor is located at the bottom of the catalyst reaction section cylinder；The position of the gas distributor is less than institute
State gas-liquid distributor.
Optionally, a diameter of 10-500mm, length 20-8000mm of the gas distributor supervisor；
The quantity of the distributor branch pipes is 1-500, a diameter of 5-300mm, length 50-5000mm；
The quantity of trepanning is 2-1000 in the distributor branch pipes, a diameter of 0.1-10mm, and percent opening is total tube section
Long-pending 10%~60%.
The distributor includes distributor supervisor, distributor branch pipes composition.
Optionally, a diameter of 20-300mm, length 50-5000mm of the gas distributor supervisor.
Optionally, the diameter upper limit of the gas distributor supervisor is selected from 15mm, 500mm；Lower limit is selected from 10mm, 15mm.
Optionally, the length limit of the gas distributor supervisor is selected from 80mm, 120mm, 180mm, 8000mm；Lower limit selects
From 20mm, 80mm, 120mm, 180mm.
Optionally, the aperture upper limit of trepanning is selected from 0.5mm, 10mm in the distributor branch pipes；Lower limit be selected from 0.1mm,
0.5mm。
Optionally, the quantity of the distributor branch pipes is 2-200, a diameter of 50-100mm, length 100-2500mm,
Each distributor branch pipes are connected with the supervisor of the distributor.
Optionally, the quantity of trepanning is 20-500 in the distributor branch pipes, and a diameter of 0.2-20mm, percent opening is total
The 20%~40% of tube section product.
Optionally, the catalyst reaction section includes gas feed mouth, liquid inlet opening and catalyst pulp outlet；
The gas feed mouth is located on the outer wall of the bottom of the catalyst reaction section cylinder, and is distributed with the gas
Device connects；
The liquid inlet opening is located at the bottom bottom of the catalyst reaction section cylinder；
The catalyst pulp exports on the outer wall of the bottom of the catalyst reaction section cylinder, position higher than the gas into
Material mouth.
Optionally, the diameter range of the catalyst reaction section cylinder is 20-10000mm, length range 100-
50000mm；
The diameter of the catalyst sedimentation section cylinder is 1.2~3.0 times of the catalyst reaction section cylinder；
The length of the catalyst sedimentation section cylinder is the 0.1~0.8 of the catalyst reaction section cylinder.
Optionally, the diameter upper limit of the catalyst reaction section cylinder be selected from 100mm, 150mm, 200mm, 5000mm,
10000mm；Lower limit is selected from 20mm, 100mm, 150mm, 200mm, 5000mm.
Optionally, the length limit of the catalyst reaction section cylinder is selected from 1000mm, 30000mm, 50000mm；Lower limit selects
From 100mm, 1000mm, 30000mm.
Optionally, the diameter of the catalyst sedimentation section cylinder of the reactor be catalyst reaction section barrel diameter 1.5~
2.0 times, length is the 0.2~0.6 of catalyst reaction section barrel lenght.There is liquid extraction filtering single in the catalyst sedimentation section
Member.
The catalyst sedimentation section of the reactor is that the flow velocity realization catalysis of reaction mixture gas liquid is reduced by enlarged diameter
While agent bulky grain settles, gas-liquid separation is had effectively achieved.
Optionally, the diameter range of the catalyst reaction section cylinder be 50~5000mm, length range be 300~
30000mm。
Optionally, the filter element is that liquid produces filter element；
The liquid extraction filter element is made of at least one set of filter and connecting tube.
The effect of the liquid extraction filter element is to realize that reaction mixture body and catalyst solid particle are realized effectively
Separation.Blowback and backwashing system are set in practical operation per set filter, filter blocks are avoided.
Optionally, at least one set of filter is in parallel；
The group number of the filter is 1-20；
A diameter of 20-500mm of the filter, length or height are 50-1000mm；
Every set filter quantity is 1~20.
Optionally, the liquid extraction filter element is made of 2~8 set filters and its connecting tube, the diameter of filter
For 50-200mm, length or height are 100-500mm, and every set filter quantity is 2~10.
Optionally, the filter is added by at least one of sintered metal wire-mesh, sintered metal powder, ceramic junction powder
Hollow cylinder or cone made of work.
Optionally, the filter is hollow cylinder or cone；
The average filtration precision of the filter is 1~50 μm.
Optionally, the average filtration precision of the filter is 5~20 μm.
Optionally, the catalyst sedimentation section further includes liquid extraction mouth；
The liquid extraction mouth is located on the outer wall of the catalyst sedimentation section cylinder；
The liquid extraction mouth is connect with the filter element.
Optionally, the reactor further includes periodic off-gases outlet and catalyst pulp import；The periodic off-gases outlet is located at
The top of the catalyst sedimentation section cylinder；
The catalyst pulp import is located on the outer wall of the catalyst sedimentation section cylinder.
Optionally, the reactor includes liquid inlet opening, gas feed mouth, liquid extraction mouth, periodic off-gases outlet, catalysis
The import of agent slurry, catalyst pulp outlet, coolant inlet, coolant outlet, catalyst reaction section cylinder, catalyst sedimentation section cylinder
Body, liquid extraction filter element, takes thermal, gas distributor at gas-liquid distributor；
The catalyst reaction section cylinder is located at the lower section of the catalyst sedimentation section cylinder.
Optionally, the reactor further includes changeover portion；
The changeover portion is between catalyst reaction section and catalyst sedimentation section；
The cross-sectional area of at least one position of the changeover portion is between at least one position of the catalyst reaction section
Between cross-sectional area and the cross-sectional area of at least one position of catalyst sedimentation section.
Optionally, the cross-sectional area of any position of the catalyst reaction section is less than any bit of the catalyst sedimentation section
The cross-sectional area set；
Cross-sectional area of the cross-sectional area of any position of the changeover portion between any position of the catalyst reaction section
Between the cross-sectional area of any position of the catalyst sedimentation section；
The changeover portion, catalyst reaction section and catalyst sedimentation section are coaxially connected.
Optionally, the cross-sectional area of at least one position of the changeover portion and any other at least one position is transversal
Area is different.
Optionally, the changeover portion includes transition section cylinder.
Optionally, the reactor includes liquid inlet opening, gas feed mouth, liquid extraction mouth, periodic off-gases outlet, catalysis
The import of agent slurry, catalyst pulp outlet, coolant inlet, coolant outlet, catalyst reaction section cylinder, catalyst sedimentation section cylinder
Body, liquid extraction filter element, takes thermal, gas distributor and transition section cylinder at gas-liquid distributor；
The catalyst reaction section cylinder is located at the lower section of the catalyst sedimentation section cylinder；The transition section cylinder is located at institute
It states between catalyst reaction section cylinder and the catalyst sedimentation section cylinder；
The cross-sectional area of at least one position of the changeover portion is between at least one position of the catalyst reaction section
Between cross-sectional area and the cross-sectional area of at least one position of catalyst sedimentation section.
Optionally, the use condition of the reactor is：Temperature is 20~200 DEG C, and pressure is 0.1~10.0MPa.
Optionally, the reactor is the three-phase bubbling bed reactor for alcohols or Oxidation of aldehydes esterification.
Optionally, the reactor is methyl methacrylate synthesis reactor.
According to the one side of the application, a kind of solution-air-liquid three-phase bubbling bed reactor, including catalysis reaction are provided
Section and two sections of cylinders of catalyst sedimentation section；Be provided in catalyst reaction section cylinder gas distributor (by distribution supervisor and branch pipe and
Distribution cap connection composition), gas-liquid distributor (being made of distribution grid and several sparger units), take thermal (it is multiple take it is hot single
Member composes in parallel), setting liquid produces filter element (being composed in parallel by multigroup filter) in catalyst sedimentation section cylinder；It is applicable in
The direct oxidation esterification of production methyl methacrylate under the conditions of 20~200 DEG C of temperature, 0.1~10.0MPa of pressure is anti-
It answers.
Setting in 50~5000mm of diameter range of the catalyst reaction section of the reactor, 300~30000mm of length range
Take thermal, gas distributor and gas-liquid distributor.
The another aspect of the application provides a kind of equipment producing methyl methacrylate, which is characterized in that comprising upper
State at least one of any one of them bubbling bed reactor.
Optionally, the equipment of the production methyl methacrylate includes above-mentioned methyl methacrylate synthesis reactor.
Optionally, the production equipment is a kind of gas, liquid, solid three-phase bubbling bed methyl methacrylate synthesis reactor.
The reactor includes catalyst reaction section and catalyst sedimentation section, and cooling device, gas-liquid distributor, gas is arranged in catalyst reaction section
Body distributor etc.；Setting liquid produces element kit etc. in catalyst sedimentation section.The reactor is suitable for temperature 20~200
DEG C, the direct oxidation esterification of the production methyl methacrylate under the conditions of 0.1~10.0MPa of pressure.
The advantageous effect that the application can generate includes：
1) present device provided herein, which can meet, uses with methacrolein, methanol and is containing oxygen gas mixture
Raw material under the action of catalyst direct oxidation esterification the characteristics of, realize the company that such oxidative esterification is strongly exothermic, easily polymerize
Continuous metaplasia production overcomes the disadvantages such as traditional raw material, catalyst and oxygen dispersion are uneven, and mass transfer effect is poor, heat transfer efficiency is low；
2) equipment provided herein can shorten simultaneously simplification of flowsheet, realize high conversion, highly selective life
Methyl methacrylate technique is produced, has compared with existing such industrialization technology and once invests low, the low competition of production cost
Advantage；
3) reactor described herein is synthesized for methyl methacrylate, obtained methyl methacrylate yield
More than 95%；Wherein, methacrolein conversion ratio is more than 99%.
Description of the drawings
Fig. 1 is the structural schematic diagram of the production equipment of the application.
Component and reference numerals list：
1- liquid inlet openings；2- gas feed mouths；3- liquid produces mouth；4- periodic off-gases export；
5- catalyst pulp imports；6- catalyst pulps export；7- cooling liquid inlets；8- cooling liquid outlets；9- catalysis is anti-
Answer a section cylinder；10- catalyst sedimentation section cylinders；11- gas-liquid distributors；12- liquid produces filter element；13- takes thermal；
14- gas distributors.
Specific implementation mode
The application is described in detail with reference to embodiment, but the application is not limited to these embodiments.
Unless otherwise instructed, the raw material in embodiments herein and catalyst are bought by commercial sources.
The computational methods of conversion ratio are as follows：
(initial amount of the reaction volume the converted/reactant) * 100%.
The computational methods of yield are as follows：
(amount of the amount of the product actually obtained/theoretically obtain product) * 100%.
The production equipment includes reactor, as shown in Figure 1, including catalyst reaction section cylinder 9 and catalyst sedimentation section cylinder
10 2 sections of cylinders of body；Gas distributor 14 is provided in catalyst reaction section cylinder (to be connected with branch pipe and distribution cap by distribution supervisor
Composition), gas-liquid distributor 11 (being made of distribution grid and several sparger units), take thermal 13 (multiple to take hot cell in parallel
Composition), setting liquid produces filter element 12 (being composed in parallel by multigroup filter) in catalyst sedimentation section cylinder.
The reactor top setting catalyst pulp import (mouth is added) 5, for device initial launch and ran
The fresh catalyst slurry that addition water configures in journey；Meanwhile it being exported (extraction mouth) in reactor lower part setting catalyst pulp
6, for producing the old catalyst in part in extraction catalyst pulp in device docking process or operational process.
In a preferred embodiment of the present invention, setting takes thermal 13 in the catalyst reaction section cylinder 9, wherein
Described to take the operation medium of thermal for coolant liquid, coolant liquid can be one of water, brine or glycol water, institute
It includes material solution, catalyst solid particle, nitrogen oxygen atmosphere and reaction product to state the operation medium in cylinder.
In a preferred embodiment of the present invention, reactor is alcohol oxidative esterification three-phase bubbling bed reactor.
In a preferred embodiment of the present invention, it is metering system that reactor, which is methyl methacrylate reaction product,
Sour methyl esters.
Cooling of the thermal for reactor is taken, by taking the realization of thermal coolant liquid quickly to reduce phlegm and internal heat, and then improves methyl
The selectivity of methyl acrylate product.
In a preferred embodiment of the present invention, it is described take thermal 13 by coolant liquid pass in and out reactor manifold and
It is multigroup that hot cell is taken to compose in parallel.
Every group takes hot cell to be made of a down-comer and several tedges；
It takes hot cell effect to be to increase cooling liquid speed, strengthens and move except the thermal efficiency, also in spallation reaction device cylinder
The rising bubbling polymerization of oxygenous gaseous mixture improves the effect of reaction efficiency at the effect of air pocket.
In a preferred embodiment of the present invention, the coolant liquid feed inlet 7 and coolant liquid discharge port 8 are arranged anti-
On the outer wall for answering device cylinder；The intake header of coolant liquid and outlet header's setting on the top of cylinder, coolant liquid by import into
Enter to be mounted on each down-comer for taking hot cell of inner barrel, and goes out back to coolant liquid after its tedge fluid interchange
Mouth manifold outflows, have the function that cooling reaction system.
In a preferred embodiment of the present invention, described that hot cell is taken to be vertically disposed at the reactor shell
It is interior, it is uniformly distributed by square, respectively take the spacing of hot cell for 50-1000mm, such as 50mm, 100mm, 200mm, 300mm, 400mm,
Arbitrary point value in the range that any two forms in 500mm, 600mm and the above point value.Respectively take the spacing between hot cell
It equal can not also wait, under preferable case, respectively take the spacing between hot cell equal.
In a preferred embodiment of the present invention, take on hot cell a down-comer diameter range is 20-
100mm, the quantity of tedge is at 2-6, and lower part is connect with down-comer, rounded uniformly distributed, a diameter of decline pipe diameter of tedge
1/6~1/4, tedge converges to form one outlet pipe in push pipe, exit duct diameter with decline pipe diameter it is identical；Take hot cell
200~6000mm of length range, single group or multigroup can be mounted on inside reactor by module.
In a preferred embodiment of the present invention, gas distributor is arranged in the catalyst reaction section bottom of the reactor
14 are connected with the gas feed mouth 2 on barrel, and mixture of feed body is formed uniform gas-liquid with feed liquid and mixed by effect
Close object；
The gas distributor includes distributor supervisor, distributor branch pipes composition.
In a preferred embodiment of the present invention, a diameter of 20-300mm of the gas distributor supervisor, length
For 50-5000mm.
In a preferred embodiment of the present invention, the quantity of the distributor branch pipes is 2-200, a diameter of 50-
100mm, length 100-2500mm, each distributor branch pipes are connected with distributor supervisor.
In a preferred embodiment of the present invention, the quantity of trepanning is 20-500 in the distributor branch pipes, directly
Diameter is 0.2-20mm, and percent opening is the 20%~40% of manifold sectional areas.
In a preferred embodiment of the present invention, gas-liquid distributor is arranged in the catalyst reaction section bottom of the reactor
11, it is made of distribution grid and distribution cap；
The working mechanism of distributor：
Gas-liquid mixture high degree of dispersion is realized using the high-ratio surface microvia interface effect of distribution cap and forms Uniform jet,
It keeps catalyst granules to suspend and realizes high efficiency mass transfer and the heat transfer of material mixed gas liquid and catalyst granules in the reactor；
In a preferred embodiment of the present invention, the allocation unit is by sintered metal wire-mesh, metal sintering powder
End, at least one hollow cylinder being process of ceramic junction powder or cone, the average pore size in allocation unit is 5~20
Between μm, percent opening is between 0.02%~1.5%；The quantity of the distribution cap is 20-1000.
In a preferred embodiment of the present invention, a diameter of 10-50mm of the distribution cap, length or height are
20-50mm, arrangement mode of the distribution cap on distribution grid are selected from least one of equilateral triangle, square, its spacing
For 40~100mm.
In a preferred embodiment of the present invention, the diameter of the catalyst sedimentation section 10 of the reactor is that catalysis is anti-
Answer section 1.5~2.0 times, length are the 0.2~0.6 of catalyst reaction section, and interior setting liquid produces filter element.
It was enlarged diameter that the catalyst sedimentation section of the reactor is logical reduces the flow velocity of reaction mixture gas liquid and realizes catalysis
While agent bulky grain settles, gas-liquid separation is had effectively achieved.
In a preferred embodiment of the present invention, liquid extraction filter element 12 by 2~8 set filters and its
Connecting tube forms, a diameter of 50-200mm of filter, and length or height are 100-500mm, and every set filter quantity is 2
~10.Liquid produces filter element 12 and is connected with the liquid extraction mouth 3 on barrel.
In a preferred embodiment of the present invention, the filter be by sintered metal wire-mesh, sintered metal powder,
At least one hollow cylinder being process or cone of ceramic junction powder, average filtration precision are 5~20 μm.
In a preferred embodiment of the present invention, the effect of the liquid extraction filter element is to realize reaction mixing
Liquid and the realization of catalyst solid particle efficiently separate.Blowback and backwashing system are set in practical operation per set filter, kept away
Exempt from filter blocks.
Embodiment 1
Using equipment shown in FIG. 1, structure of reactor：
Reactor catalysis conversion zone：Cylinder height 1000mm, a diameter of 100mm；
Inner barrel setting is as follows：
1. taking hot cell：It is vertically positioned in the reactor cylinder body；Quantity is 1 group, length 800mm, declines pipe diameter
For 20mm, rise pipe diameter 6mm, quantity 4, the total pipe diameter 20mm of tedge；
2. gas distributor：A diameter of 10mm of supervisor；Length is 80mm；
A diameter of 5mm of branch pipe, quantity are 4；
Open pore size is 0.5mm on branch pipe；Number of aperture is 12；
3. gas-liquid distributor：A diameter of 100mm of distribution grid；
Distribution grid has distribution cap：Quantity is 8；For sintered metal wire-mesh hollow cylinder；
Average pore size on distribution grid is 0.02mm；Percent opening is 0.05%；
The a diameter of 5mm for distributing cap, is highly 10mm；
It is equilateral triangle, its spacing 15mm to distribute arrangement mode of the cap on distribution grid.
Reactor catalysis settling section：Cylinder height 500mm, a diameter of 200mm；
Inner barrel setting is as follows：
Liquid produces filter element：It is made of 1 set filter and its connecting tube, a diameter of 50mm of filter, length is
200mm, every set filter quantity is 4.
Filter is the hollow cylinder being process by sintered metal wire-mesh, and average filtration precision is 5 μm.
The aqueous solution that catalyst solid particle (nanogold) 30% will be contained is added in reactor, in reactor catalysis conversion zone
Establish 80% liquid level；
By material solution (methacrolein, methanol, water, lye (magnesium hydroxide), the resistance of certain temperature, pressure and flow
Poly- agent (1,4- ethyl tert-butyl -4,2- nitrosophenols) continuously enters from the liquid inlet opening of reactor bottom 1 in reactor；
Unlatching takes thermal, takes thermal to be passed through coolant to reactor, and establish cycle；
Certain temperature, pressure and flow are continuously entered instead from the gas feed mouth 2 of reactor bottom containing oxygen gas mixture
It answers in device；
The oxidative esterification reaction of methacrolein is carried out in reactor at this time；
It is unreacted to be continuously discharged from the periodic off-gases of reactor head outlet 4 containing oxygen gas mixture；
Reaction mixture body is discharged through liquid filter element from liquid extraction mouth.
Apparatus and process condition is as follows：
Reaction temperature：70 DEG C, reaction pressure is 0.4MPa (A)
Material solution forms and mass content：Methacrolein, 20%；Methanol, 20%；Water, 60%
Polymerization inhibitor：20ppm；PH value, 7.5
Composition and volume content of the raw material containing oxygen gas mixture：Nitrogen, 80%；Oxygen 20%；
Reaction result：
Methacrolein conversion ratio：99.2%.
Methyl methacrylate yield：95.6%.
Embodiment 2
Using equipment shown in FIG. 1, structure of reactor：
Reactor catalysis conversion zone：Cylinder height 1000mm, a diameter of 150mm；
Inner barrel setting is as follows：
1. taking hot cell：It is vertically positioned in the reactor cylinder body；Quantity is 1 group, length 800mm, declines pipe diameter
For 25mm, rise pipe diameter 6mm, quantity 6, the total pipe diameter 20mm of tedge；
2. gas distributor：A diameter of 15mm of supervisor；Length is 120mm；
A diameter of 5mm of branch pipe, quantity are 6；
Open pore size is 0.5mm on branch pipe；Number of aperture is 24；
3. gas-liquid distributor：A diameter of 150mm of distribution grid；
Distribution grid has distribution cap：Quantity is 16；For sintered metal wire-mesh hollow cylinder；
Average pore size on distribution grid is 0.02mm；Percent opening is 0.05%；
The a diameter of 5mm for distributing cap, is highly 10mm；
It distributes arrangement mode of the cap on distribution grid to be square, its spacing 15mm.
Reactor catalysis settling section：Cylinder height 500mm, a diameter of 300mm；
Inner barrel setting is as follows：
Liquid produces filter element：It is made of 1 set filter and its connecting tube, a diameter of 50mm of filter is highly
200mm, every set filter quantity is 6.
Filter is the cone being process by sintered metal powder, and average filtration precision is 5 μm.
The aqueous solution that catalyst solid particle (nanogold) 30% will be contained is added in reactor, in reactor catalysis conversion zone
Establish 80% liquid level；
By material solution (methacrolein, methanol, water, lye (magnesium hydroxide), the resistance of certain temperature, pressure and flow
Poly- agent (1,4- ethyl tert-butyl -4,2- nitrosophenols) continuously enters from the liquid inlet opening of reactor bottom 1 in reactor；
Unlatching takes thermal, takes thermal to be passed through coolant to reactor, and establish cycle；
Certain temperature, pressure and flow are continuously entered instead from the gas feed mouth 2 of reactor bottom containing oxygen gas mixture
It answers in device；
The oxidative esterification reaction of methacrolein is carried out in reactor at this time；
It is unreacted to be continuously discharged from the periodic off-gases of reactor head outlet 4 containing oxygen gas mixture；
Reaction mixture body is discharged through liquid filter element from liquid extraction mouth.
Apparatus and process condition is as follows：
Reaction temperature：80 DEG C, reaction pressure is 0.5MPa (A)
Material solution forms and mass content：Methacrolein, 20%；Methanol, 20%；Water, 60%
Polymerization inhibitor：20ppm；PH value, 8.0
Composition and volume content of the raw material containing oxygen gas mixture：Nitrogen, 80%；Oxygen 20%；
Reaction result：
Methacrolein conversion ratio：99.6%.
Methyl methacrylate yield：97.5%.
Embodiment 3
Using equipment shown in FIG. 1, structure of reactor：
Reactor catalysis conversion zone：Cylinder height 1000mm, a diameter of 200mm；
Inner barrel setting is as follows：
1. taking hot cell：It is vertically positioned in the reactor cylinder body；Quantity is 1 group, length 800mm, declines pipe diameter
For 40mm, rise pipe diameter 6mm, quantity 8, the total pipe diameter 40mm of tedge；
2. gas distributor：A diameter of 15mm of supervisor；Length is 180mm；
A diameter of 5mm of branch pipe, quantity are 8；
Open pore size is 0.5mm on branch pipe；Number of aperture is 36；
3. gas-liquid distributor：A diameter of 200mm of distribution grid；
Distribution grid has distribution cap：Quantity is 36；For sintered metal wire-mesh hollow cylinder；
Average pore size on distribution grid is 0.02mm；Percent opening is 0.05%；
The a diameter of 5mm for distributing cap, is highly 10mm；
It is its spacing to distribute arrangement side of the cap on distribution grid, its spacing 15mm.
Reactor catalysis settling section：Cylinder height 500mm, a diameter of 400mm；
Inner barrel setting is as follows：
Liquid produces filter element：It is made of 1 set filter and its connecting tube, a diameter of 50mm of filter, length is
200mm, every set filter quantity is 10.
Filter is the hollow cylinder being process by ceramic junction powder, and average filtration precision is 5 μm.
The aqueous solution that catalyst solid particle (nanogold) 30% will be contained is added in reactor, in reactor catalysis conversion zone
Establish 80% liquid level；
By material solution (methacrolein, methanol, water, lye (magnesium hydroxide), the resistance of certain temperature, pressure and flow
Poly- agent (1,4- ethyl tert-butyl -4,2- nitrosophenols) continuously enters from the liquid inlet opening of reactor bottom 1 in reactor；
Unlatching takes thermal, takes thermal to be passed through coolant to reactor, and establish cycle；
Certain temperature, pressure and flow are continuously entered instead from the gas feed mouth 2 of reactor bottom containing oxygen gas mixture
It answers in device；
The oxidative esterification reaction of methacrolein is carried out in reactor at this time；
It is unreacted to be continuously discharged from the periodic off-gases of reactor head outlet 4 containing oxygen gas mixture；
Reaction mixture body is discharged through liquid filter element from liquid extraction mouth.
Apparatus and process condition is as follows：
Reaction temperature：90 DEG C, reaction pressure is 0.6MPa (A)
Material solution forms and mass content：Methacrolein, 30%；Methanol, 30%；Water, 40%
Polymerization inhibitor：30ppm；PH value, 8.0
Composition and volume content of the raw material containing oxygen gas mixture：Nitrogen, 85%；Oxygen 15%；
Reaction result：
Methacrolein conversion ratio：99.7%.
Methyl methacrylate yield：95.8%.
Embodiment 4
The difference of reactor and reactor described in embodiment 1 in the present embodiment is：
1. it includes transition section cylinder to have changeover portion, the changeover portion between reactor catalysis conversion zone and catalysis settling section；
The diameter of the transition section cylinder is between the diameter and the diameter of catalysis settling section cylinder of catalyst reaction section cylinder.
2. taking hot cell：It is vertically positioned in the reactor cylinder body；Quantity is 4 groups, uniformly distributed by square, respectively takes hot cell
Spacing be 2000mm.
Other are same as Example 1.
The above is only several embodiments of the application, not does any type of limitation to the application, although this Shen
Please disclosed as above with preferred embodiment, however not to limit the application, any person skilled in the art is not taking off
In the range of technical scheme, makes a little variation using the technology contents of the disclosure above or modification is equal to
Case study on implementation is imitated, is belonged in technical proposal scope.
Claims (10)
1. a kind of bubbling bed reactor, which is characterized in that the reactor includes catalyst reaction section and catalyst sedimentation section；
The cross-sectional area of at least one position of the catalyst reaction section is less than at least one position of the catalyst sedimentation section
Cross-sectional area；
The catalyst reaction section is located at the lower section of the catalyst sedimentation section.
2. reactor according to claim 1, which is characterized in that the cross-sectional area of any position of the catalyst reaction section
Less than the cross-sectional area of any position of the catalyst sedimentation section；
The catalyst reaction section and catalyst sedimentation section are coaxially connected；
Preferably, the length of the catalyst sedimentation section is less than the length of the catalyst reaction section；
Preferably, the diameter range of the catalyst reaction section is 20~10000mm, and length range is 100~50000mm；
The diameter of the catalyst sedimentation section is 1.2~3.0 times of catalyst reaction section diameter, and length is catalyst reaction section length
0.1~0.8；
Preferably, include taking thermal, gas distributor and gas-liquid distributor in the catalyst reaction section；
The catalyst sedimentation section includes liquid extraction filter element.
3. reactor according to claim 1, which is characterized in that the catalyst reaction section include catalyst reaction section cylinder,
Take thermal, gas-liquid distributor, gas distributor；Wherein, it is described take thermal, gas-liquid distributor and gas distributor be located at urge
Change in conversion zone cylinder；
The catalyst sedimentation section includes catalyst sedimentation section cylinder, filter element；Wherein, the filter element is located at catalyst
In settling section cylinder；
Preferably, the catalyst reaction section cylinder and catalyst sedimentation section cylinder coaxial communication；The catalyst reaction section cylinder
Diameter is less than the diameter of catalyst sedimentation section cylinder；
It is preferably, described that take thermal include at least one set of taking the outlet of hot cell, the intake header of coolant liquid and coolant liquid total
Pipe；
Wherein, the outlet header of the intake header for taking hot cell and coolant liquid and coolant liquid connects；
The intake header of the coolant liquid and the outlet header of coolant liquid are located at the top of the catalyst reaction section cylinder；
The intake header of the coolant liquid the import of reactor, the coolant liquid outlet header in the equal position in the outlet of reactor
In on the outer wall of the catalyst reaction section cylinder；
Preferably, it includes a down-comer and at least one tedge that described one group, which takes hot cell,；
The lower part of the tedge is connect with down-comer, rounded to be uniformly distributed；The tedge converges to form one in push pipe
Outlet, exit duct diameter are identical as pipe diameter is declined；
Wherein, the down-comer is connect with the intake header of the coolant liquid；The tedge and the outlet of the coolant liquid are total
Pipe connects；
Preferably, the diameter range of the down-comer is 10-200mm；
The quantity of the tedge is at 1-10；
The a diameter of 1/8-1/2 for declining pipe diameter of the tedge；
Preferably, it is parallel connection that at least one set, which takes hot cell,；
It is described to take the length of hot cell for 100~10000mm；
It is described that hot cell is taken to be vertically positioned in the catalyst reaction section cylinder, it is uniformly distributed by square, between respectively taking between hot cell
Away from for 20-2000mm；
Preferably, the gas-liquid distributor includes distribution grid and distribution cap；The gas-liquid distributor is located at the catalyst reaction section
The bottom of cylinder；
Preferably, for the average pore size on the distribution grid between 1~50 μm, percent opening is 0.01%~2.0%；
The quantity of the distribution cap is 10-5000；
A diameter of 5-100mm of the distribution cap, length or height are 5-100mm；
The distribution cap is hollow cylinder or cone；
Arrangement mode of the distribution cap on distribution grid is selected from least one of equilateral triangle, square, and arrangement spacing is
15~200mm；
Preferably, the gas distributor includes distributor supervisor and distributor branch pipes, each distributor branch pipes and the distributor
Supervisor be connected；
The gas distributor is located at the bottom of the catalyst reaction section cylinder；The position of the gas distributor is less than the gas
Liquid distributor；
Preferably, a diameter of 10-500mm, length 20-8000mm of the gas distributor supervisor；
The quantity of the distributor branch pipes is 1-500, a diameter of 5-300mm, length 50-5000mm；
The quantity of trepanning is 2-1000 in the distributor branch pipes, a diameter of 0.1-10mm, and percent opening is manifold sectional areas
10%~60%；
Preferably, the catalyst reaction section includes gas feed mouth, liquid inlet opening and catalyst pulp outlet；
The gas feed mouth is located on the outer wall of the bottom of the catalyst reaction section cylinder, and connects with the gas distributor
It connects；
The liquid inlet opening is located at the bottom bottom of the catalyst reaction section cylinder；
The catalyst pulp exports on the outer wall of the bottom of the catalyst reaction section cylinder, and position is higher than the gas feed
Mouthful；
Preferably, the diameter range of the catalyst reaction section cylinder is 20-10000mm, length range 100-50000mm；
The diameter of the catalyst sedimentation section cylinder is 1.2~3.0 times of the catalyst reaction section barrel diameter；
The length of the catalyst sedimentation section cylinder is the 0.1~0.8 of the catalyst reaction section barrel lenght；
Preferably, the diameter range of the catalyst reaction section cylinder is 50~5000mm, and length range is 300~30000mm；
Preferably, the filter element is that liquid produces filter element；
The liquid extraction filter element is made of at least one set of filter and connecting tube；
Preferably, it is in parallel between at least one set of filter；
The group number of the filter is 1-20；
A diameter of 20-500mm of the filter, length or height are 50-1000mm；
Every set filter quantity is 1~20；
Preferably, the filter is hollow cylinder or cone；
The average filtration precision of the filter is 1~50 μm；
Preferably, the catalyst sedimentation section further includes liquid extraction mouth；
The liquid extraction mouth is located on the outer wall of the catalyst sedimentation section cylinder；
The liquid extraction mouth is connect with the filter element；
Preferably, the reactor further includes periodic off-gases outlet and catalyst pulp import；
The periodic off-gases outlet is positioned at the top of the catalyst sedimentation section cylinder；
The catalyst pulp import is located on the outer wall of the catalyst sedimentation section cylinder.
4. reactor according to claim 1, which is characterized in that the reactor includes liquid inlet opening, gas feed
Mouthful, liquid extraction mouth, periodic off-gases outlet, catalyst pulp import, catalyst pulp outlet, coolant inlet, coolant outlet,
Catalyst reaction section cylinder, gas-liquid distributor, liquid extraction filter element, takes thermal, gas distribution at catalyst sedimentation section cylinder
Device；
The catalyst reaction section cylinder is located at the lower section of the catalyst sedimentation section cylinder.
5. reactor according to claim 1, which is characterized in that the reactor further includes changeover portion；
The changeover portion is between catalyst reaction section and catalyst sedimentation section；
The cross-sectional area of at least one position of the changeover portion is transversal between at least one position of the catalyst reaction section
Between area and the cross-sectional area of at least one position of catalyst sedimentation section；
Preferably, the cross-sectional area of any position of the catalyst reaction section is less than any position of the catalyst sedimentation section
Cross-sectional area；
Cross-sectional area and institute of the cross-sectional area of any position of the changeover portion between any position of the catalyst reaction section
Between the cross-sectional area for stating any position of catalyst sedimentation section；
The changeover portion, catalyst reaction section and catalyst sedimentation section are coaxially connected；
Preferably, the cross-sectional area of the cross-sectional area of at least one position of the changeover portion and any other at least one position
It is different；
Preferably, the changeover portion includes transition section cylinder.
6. reactor according to claim 1, which is characterized in that the reactor includes liquid inlet opening, gas feed
Mouthful, liquid extraction mouth, periodic off-gases outlet, catalyst pulp import, catalyst pulp outlet, coolant inlet, coolant outlet,
Catalyst reaction section cylinder, gas-liquid distributor, liquid extraction filter element, takes thermal, gas distribution at catalyst sedimentation section cylinder
Device and transition section cylinder；
The catalyst reaction section cylinder is located at the lower section of the catalyst sedimentation section cylinder；
The transition section cylinder is between the catalyst reaction section cylinder and the catalyst sedimentation section cylinder；
The cross-sectional area of at least one position of the changeover portion is transversal between at least one position of the catalyst reaction section
Between area and the cross-sectional area of at least one position of catalyst sedimentation section.
7. reactor according to claim 1, which is characterized in that the use condition of the reactor is：Temperature be 20~
200 DEG C, pressure is 0.1~10.0MPa.
8. reactor according to any one of claims 1 to 7, which is characterized in that the reactor is for alcohols or aldehyde
The three-phase bubbling bed reactor of class oxidative esterification reaction.
9. reactor according to any one of claims 1 to 7, which is characterized in that the reactor is methyl methacrylate
Ester synthesis reaction device.
10. a kind of equipment producing methyl methacrylate, which is characterized in that roused comprising claim 1 to 7 any one of them
Steep at least one of bed reactor.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810218237.5A CN108380141A (en) | 2018-03-16 | 2018-03-16 | Bubbling bed reactor, methyl methacrylate production equipment |
| PCT/CN2018/080017 WO2019174064A1 (en) | 2018-03-16 | 2018-03-22 | Bubbling bed reactor and methyl methacrylate production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810218237.5A CN108380141A (en) | 2018-03-16 | 2018-03-16 | Bubbling bed reactor, methyl methacrylate production equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108380141A true CN108380141A (en) | 2018-08-10 |
Family
ID=63066568
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810218237.5A Pending CN108380141A (en) | 2018-03-16 | 2018-03-16 | Bubbling bed reactor, methyl methacrylate production equipment |
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| Country | Link |
|---|---|
| CN (1) | CN108380141A (en) |
| WO (1) | WO2019174064A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111036150A (en) * | 2019-12-02 | 2020-04-21 | 河南金鹏化工有限公司 | Process and device for continuously producing thiodicarb by alcohol washing |
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| CN1158624A (en) * | 1994-08-02 | 1997-09-03 | 联合碳化化学品及塑料技术公司 | Gas phase polymerization process |
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| CN201529518U (en) * | 2009-05-13 | 2010-07-21 | 中国石油化工股份有限公司 | Gas-liquid-solid three-phase fixed bubbling column reactor |
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| CN111036150B (en) * | 2019-12-02 | 2023-07-25 | 河南金鹏化工有限公司 | Thiodicarb alcohol washing continuous production process and device |
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| Publication number | Publication date |
|---|---|
| WO2019174064A1 (en) | 2019-09-19 |
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